RU2623433C2 - Ethylene removal by absorption - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: method comprises: light gas stream separation from the polymerization product stream, at that, the said light gas stream comprises unreacted ethylene; light gas stream contacting with the absorbing solvent system, this contacting light gas stream with the absorbent solvent system is performed at a temperature in the range of 4°C (40°F) to 43°C (110°F). At least a part of the unreacted ethylene from the light gas stream is absorbed by the absorbent solvent system; and unreacted ethylene is recovered from the absorbent solvent system to obtain the recovered ethylene. The absorbent solvent system comprises copper chloride, aniline and N-methylpyrrolidone. The invention also relates to a process for preparation of polyethylene and three versions of the polyethylene production system.

EFFECT: invention enables high efficiency of ethylene separation from the recycling stream.

34 cl, 10 dwg, 3 tbl, 41 ex

Description

CROSS RELATIONS TO RELATED APPLICATIONS

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

BACKGROUND

Technical field

[0002] The present invention generally relates to the production of polyethylene. In particular, the present invention relates to systems and methods for improving the efficiency of polyethylene production by reducing ethylene losses.

State of the art

[0003] The production of polymers, such as polyethylene, from light gases requires highly pure raw materials of monomers and comonomers. Due to small differences in the boiling points between light gases in such raw materials, the industrial production of such high-purity raw materials may require the operation of many distillation columns, high pressures and cryogenic temperatures. For this reason, the energy costs associated with the purification of raw materials represent a significant part of the total cost of production of these polymers. In addition, the infrastructure necessary for the production, storage and recycling of high-purity raw materials makes up a significant part of the associated capital investments.

[0004] To compensate for some of the costs and maximize production, it may be useful to return and / or recycle any unreacted feed gases, especially light hydrocarbon reagents such as ethylene. Gases containing unreacted monomers can be separated from the polymer after the polymerization reaction. The polymer is recycled, while unreacted monomers are recovered from the gases returned from the polymerization reaction. To carry out these operations, the return gas streams were usually either subjected to a purification process or redirected to other duplicate processing steps. In both cases, traditional methods for the extraction of monomer led to the necessity of using energetically disadvantageous and expensive methods.

[0005] Therefore, there is a need for a highly efficient separation of ethylene from a recycling stream.

SUMMARY OF THE INVENTION

[0006] The present invention describes a method for extracting ethylene from a polymerization product stream of a polyethylene production system, comprising separating a light gas stream from a polymerization product stream, said light gas stream comprising ethane and unreacted ethylene, contacting the light gas stream with an absorbent solvent system, moreover, bringing into contact the flow of light gases with a system of absorbent solvents is carried out at a temperature in the range from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), m at least part of the unreacted ethylene from light gases stream is absorbed solvents absorbent system and recovering unreacted ethylene from the system of absorbent solvent to obtain the recovered ethylene.

[0007] In addition, the present application describes a method for producing polyethylene, comprising contacting ethylene and a polymerization catalyst in a polymerization reactor under suitable reaction conditions to form a polymerization product stream, separating the light gas stream from the polymerization product stream, wherein said light gas stream contains unreacted ethylene, contacting the light gas stream with an absorbent solvent system in an absorption reactor at a temperature in the range of about 4 ° C (40 ° F) ) to about 43 ° C (110 ° F), at least a portion of the unreacted ethylene from the light gas stream is absorbed by the absorbent solvent system to form a composition comprising a complex of the absorbent solvent system and unreacted ethylene, removing unabsorbed gases from the light gas stream after being brought into contacting the absorbent solvent system, recovering unreacted ethylene from the absorbent solvent system, and contacting the recovered ethylene with the catalyst floor imizatsii.

[0008] Also disclosed herein is a polyethylene production system comprising a feed stream containing ethylene, said feed stream being characterized by being included in a polymerization reactor, a stream of polymerization products, said stream of polymerization products being characterized by leaving the polymerization reactor and enters the separator, a stream of light gases containing unreacted ethylene, wherein said stream of light gases is characterized by the fact that it leaves the separator, in which the stream of light the basics were separated from the polymerization product stream, said light gas stream being characterized by being included in an absorbent solvent system, said absorbent solvent system having a temperature in the range of about 4 ° C (40 ° F) to about 43 ° C (110 ° F), an ethylene absorbent conjugate, wherein said ethylene absorbent conjugate is characterized in that it is formed within an absorbent solvent system by absorbing at least a portion of unreacted ethylene with an absorbent system x solvents, and an exhaust stream containing ethane, wherein said exhaust stream is characterized in that it leaves the absorption reactor, said exhaust stream comprising components of a light gas stream not absorbed by an absorbent solvent system, and a stream of recovered unreacted ethylene, wherein said stream of recovered unreacted ethylene is characterized in that it leaves the absorption reactor and re-enters the polymerization reactor.

[0009] Also disclosed herein is a polyethylene production system including a polymerization reactor, said polymerization reactor configured to receive a feed stream containing ethylene, said polymerization reactor configured to discharge a polymerization product stream, a separator, wherein said separator is configured to receive a stream of polymerization products and release a stream of light gases containing unreacted ethylene, and the specified stream of light gases was separated from the polymerization product stream, and an absorption reactor containing an absorbent solvent system, said absorption reactor configured to receive a stream of light gases, absorb at least a portion of unreacted ethylene by an absorbent solvent system at a temperature in the range of about 4 ° C (40 ° F) ) to about 43 ° C (110 ° F), and discharging an exhaust gas stream containing components of a light gas stream that have not been absorbed by an absorbent solvent system, wherein seemed absorbent reactor is further adapted to produce a stream of recovered unreacted ethylene, said polymerization reactor is further adapted to receive a flow of the recovered unreacted ethylene.

[0010] Also disclosed herein is a polyethylene production system including a polymerization reactor, wherein said polymerization reactor is configured to receive a feed stream containing ethylene, said polymerization reactor configured to discharge a polymerization product stream, a separator, wherein said separator is configured to receive a stream of polymerization product and release a stream of light gases containing unreacted ethylene, and the specified stream of light gases was from divided from the stream of polymerization products, an absorption reactor containing an absorbent solvent system, said absorption reactor configured to receive a stream of light gases, absorb at least a portion of unreacted ethylene using an absorbent solvent system at a temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F) and discharging an exhaust gas stream containing light gas stream components not absorbed by an absorbent solvent system, and ny absorption reactor is further adapted to produce an integrated stream containing ethylene is absorbed in the system of absorbent solvents and solvent regenerator for regeneration system of absorbent solvent and for discharging the stream of recovered unreacted ethylene, said polymerization reactor is further adapted to receive a flow of the recovered unreacted ethylene.

[0011] The features and technical advantages of the subject matter of the present invention have been broadly described above to better understand the following detailed description. The various characteristics described above, as well as other features, will be readily apparent to those skilled in the art after reading the following detailed description of preferred embodiments, with reference to the accompanying drawings.

DESCRIPTION OF DRAWINGS

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

[0013] FIGURE 1 illustrates a diagram of a first embodiment of a polyethylene production system;

[0014] FIGURE 2 illustrates a diagram of a second embodiment of a polyethylene production system;

[0015] FIGURE 3 illustrates a diagram of a third embodiment of a polyethylene production system;

[0016] FIGURE 4 illustrates a process flow diagram of a first embodiment of a method for producing polyethylene;

[0017] FIGURE 5 illustrates a process flow diagram of a second embodiment of a method for producing polyethylene;

[0018] FIGURE 6 illustrates a process flow diagram of a third embodiment of a method for producing polyethylene;

[0019] FIGURE 7 is a graph showing temperature solubility for ethylene and ethane in an absorbent solvent system;

[0020] FIGURE 8 illustrates a diagram of an embodiment of an absorption reactor having a pressure differential absorption configuration;

[0021] FIGURE 9 illustrates a diagram of an embodiment of an adsorption system; and

[0022] FIGURE 10 illustrates a diagram of an embodiment of an adsorption system model.

DETAILED DESCRIPTION OF THE INVENTION

[0023] This application describes systems, installations and methods related to the production of polyethylene with increased efficiency. Systems, plants, and methods generally relate to separating a first chemical component or compound from a composition obtained in the production of polyethylene and containing the first chemical component or compounds and one or more other chemical components, compounds, or similar components.

[0024] Figure 1 describes the first polyethylene production system (PES) 100. The PES system 100 generally includes a purifier 102, reactors 104, 106, a separator 108, a processor 110, an absorption reactor 116, and a processing device 114. In embodiments of the PES according to the present The description of the various components of the system can be in fluid communication through one or more conductors (for example, pipes, hoses, fluid supply lines, etc.) suitable for transmitting a particular stream, for example, as shown in detail numbered flows in Figures 1-3.

[0025] In the embodiment shown in Figure 1, the feed stream 10 can be transferred to a purifier 102. The stream of purified feed 11 can be transferred from the purifier 102 to one or more reactors 104, 106. If the system includes two or more reactors, the reactor stream 15 can be transferred from reactor 104 to reactor 106. The stream of polymerization products 12 can be transferred from one or more reactors 104, 106 to a separator 108. The polymer stream 14 can be transferred from a separator 108 to a processor 110. The product stream 16 can be discharged from a processor 110. Gas stream 18 can transfer from separator 108 to absorption reactor 116. Exhaust gas stream 20 can be transferred from absorption reactor 116 to processing device 114, and recycle stream 22 can be transferred from absorption reactor 116 to separator 108. Re-introduced stream 24 can be transferred from separator 108 to purifier 102 .

[0026] Figure 2 describes a second embodiment of a PPE 200 production system, some of whose components are common with PPE 100. In the alternative embodiment shown in Figure 2, the second PPE 200 system further includes an oxygen removal device 118. As an alternative to the first PPE system 100 (shown in FIG. 1), in the embodiment shown in FIG. 2, the gas stream 18 can be transferred to the oxygen removal device 118. The processed gas stream 26 can be transferred from the oxygen removal device 118 to the absorption reactor 1 16.

[0027] Figure 3 describes a second embodiment of a PPE 300 production system, some of whose components are common with PPE 100 and PPE 200. In the alternative embodiment shown in Figure 3, the second PPE 300 further includes a regenerator 120 (eg, a desorption vessel) . As an alternative to the first and second PES systems 100 and 200, respectively, in the embodiment shown in FIG. 3, the complex stream 28 can be transferred from the absorption reactor 116 to the regenerator 120. The recycle stream 22 can be transferred from the regenerator 120 to the separator 108, and the regenerated stream absorbent 30 may be transferred from regenerator 120 to absorption reactor 116.

[0028] In Figure 3, the temperature of the regenerated solvent can be obtained from stream 30. 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 thermal effect of dissolution, and the thermal effect of the reaction. In the described embodiments, the mass flow rate of the regenerated solvent in stream 30 can be 50-300 times the mass flow rate of the gas stream 18. Therefore, the temperature in the adsorption reactor 116 can significantly depend on the temperature of the regenerated solvent in the described embodiments.

[0029] Various suitable implementations of a PES system have been described, further embodiments of a PES method are described. One or more embodiments of the PES method can be described with reference to one or more systems from the PES system 100, the PES system 200 and / or the PES system 300. Although this PES method can be described with reference to one or more embodiments of the PES system, such a description should not be construed as limited to these options. Although the various steps of the methods of the present invention can be described or illustrated in a specific order, this should not be construed as limiting these methods in any particular order, unless otherwise indicated.

[0030] Figure 4 shows the first method of PES 400. The method of PES 400 generally includes block 51 purifying the feed stream, block 52 polymerizing the monomers of the purified feed stream to form a polymerization product, and in block 53 separating the polymerization product into a polymer stream and gas stream , in block 54, processing the polymer stream, in block 55, separating at least one gaseous component from the gas stream to form a recycle stream and a waste stream, and in block 56 burning the waste stream.

[0031] In one embodiment, the first PES method 400 or part of the method can be implemented by the first PES system 100 (for example, as shown in FIG. 1). In figures 1 and 4 in one embodiment, the implementation of the feed stream 10 may contain a gaseous reactant, in particular ethylene. In one embodiment, purification of the feed stream results in a purified stream 11 containing substantially pure monomers (e.g., ethylene monomers), comonomers (e.g., butene-1 comonomers), or combinations of these compounds. Polymerization of the monomers (optionally comonomers) of the purified stream 11 results in a polymerization product stream 12 generally containing unreacted monomer (e.g. ethylene), optionally unreacted comonomer (e.g. butene-1), by-products (e.g. ethane, which can represent failure ethane, formed as a by-product of ethylene and hydrogen) and a polymerization product (for example, a polymer and, optionally, a copolymer). Separation of the polymerization product stream 12 results in a polymer stream 14 (for example, a polyethylene polymer, a copolymer) and a gas stream 18 generally containing unreacted monomer (for example, ethylene monomer and optionally a comonomer such as butene-1) and various exhaust gases (e.g. ethane). Processing the polymer stream 14 results in a product stream 16. The separation of at least one gaseous component from the gas stream 18 results in a recycle stream 22, generally containing unreacted ethylene monomer (optionally unreacted comonomer), and an exhaust stream 20. In one of the embodiments, separation of the gas stream 18 includes absorption of ethylene from the gas stream 18 to produce an exhaust gas stream 20, and then releasing the absorbed ethylene to form the circulating stream 22. The recycled stream 22 containing ethylene can be compressed (for example, returned to the separator 108 for compression) and re-introduced into the PES method (for example, the PES method 400) in the form of a re-introduced stream 24. Burning of the exhaust gas stream 20 can be carried out using a torch, such as a recycling device 114.

[0032] FIG. 5 shows a second PES method 500, which has a number of common steps with the PES method 400. In the alternative embodiment shown in FIG. 5, block 55 of FIG. 4 is improved by introducing a block 57 that processes the gas stream to form a treated gas flow, and in block 55 ', at least one component of the treated gas stream is separated to form a recycle stream and an exhaust stream.

[0033] In one embodiment, the second PES method 500 or part of it can be implemented by the second PES system 200 (for example, as shown in FIG. 2). As an alternative to the embodiments of FIGS. 1 and 4, in the embodiment of FIGS. 2 and 5, processing the gas stream 18 results in a processed gas stream 26. In one embodiment, processing the gas stream 18 includes removing oxygen from the gas stream 18. Separation of at least one gaseous component from the treated gas stream 26 results in a recycle stream 22 generally containing unreacted ethylene monomer (optionally a comonomer) and an exhaust gas stream 20.

[0034] FIG. 6 shows a third PES method 600, which has a number of common steps with the PES method 500. In the alternative embodiment shown in FIG. 6, block 55ʹ of figure 5 is improved due to the separation of at least one block 55ʹʹ the gaseous component from the treated gas stream to form a complex stream and an exhaust stream, and due to the introduction of block 58, in which the complex stream is divided into an absorbent stream and a recycle stream.

[0035] In one embodiment, the third PES method 600 or part thereof can be implemented by a third PES system 300 (for example, as shown in FIG. 3). As an alternative to the embodiments of FIGS. 1 and 4 and 2 and 5, in the embodiment of FIGS. 3 and 6, separating at least one gaseous component from the treated gas stream 26 results in an unreacted absorbent monomer (e.g., ethylene absorbent) in complex stream 28. In one embodiment, separating the complex stream unreacted absorbent monomer 28 includes releasing the absorbed ethylene to form a recycle stream 22 and a regenerated absorb nta 30. In the embodiment of FIGS. 3 and 6, separating at least one gaseous component from the treated gas stream 26 results in unreacted absorbent comonomer (eg, butene-1 absorbent) in the complex stream 28. In one embodiment separating the unreacted absorbent comonomer in the complex stream 28 includes releasing the absorbed comonomer to form a recycle stream 22 and a regenerated absorbent stream 30.

[0036] In one or more embodiments as described herein, purification of a feed stream (eg, in block 51) may include separating undesired compounds and elements from a feed stream containing ethylene to form a stream of purified feed. In one embodiment, the feed stream may comprise ethylene and various other gases, such as, without limitation, methane, ethane, acetylene, propylene, various other hydrocarbons containing three or more carbon atoms, or combinations of these gases. In one embodiment, purification of the feed stream may include any suitable method or process, including but not limited to filtering, passing through a membrane, reacting with various chemicals, absorption, adsorption, distillation (distillation), or combinations of these methods.

[0037] In the implementations shown in figures 1-3, the purification of the feed stream may include directing the flow of raw materials 10 to the cleaner 102. In one or more embodiments of the present description, the cleaner 102 may include a device or installation suitable for cleaning one or more gaseous reactants in a feed stream containing many potentially undesirable gaseous compounds, elements, impurities or similar components. 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 of these cleaners. Purifier 102 may be configured to separate ethylene from a stream containing methane, ethane, acetylene, propane, propylene, water, oxygen, other various gaseous hydrocarbons, various impurities and / or combinations of these compounds.

[0038] In one embodiment, purification of the feed stream results in a purified feed 11 containing substantially pure ethylene. In one embodiment, the refined feed stream may contain less than about 25% of the total mass of the stream, alternatively, less than about 10%, alternatively, less than about 1.0% of one or more of the following gases: nitrogen, oxygen, methane, ethane, propane or combinations of these gases. As used herein, “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 about 90% ethylene, alternatively at least about 95% ethylene, alternatively at least about 99% ethylene, based on the total weight of the stream, alternatively at least about 99.5% ethylene, on the total weight of the stream. In one embodiment, the feed stream 11 may further comprise trace amounts of ethane, for example, from a recycle stream, which will be discussed later.

[0039] In one or more embodiments as described herein, polymerizing the monomers of the purified feed (eg, in block 52) may include allowing the polymerization reaction to occur between the plurality of monomers by contacting the monomer or monomers with the catalyst system under conditions suitable for polymer formation . In one or more embodiments as described herein, the polymerization of comonomers (e.g., in block 52) may include allowing the polymerization reaction to occur between the plurality of comonomers by contacting the comonomer or comonomers with the catalyst system under conditions suitable for the formation of the copolymer. In one embodiment, any suitable catalyst system may be used. A suitable catalyst system may include a catalyst and, optionally, a cocatalyst and / or promoter. Non-limiting examples of suitable catalyst systems include Ziegler-Natta catalysts, Ziegler catalysts, chromium catalysts, chromium catalysts, chromocene catalysts, metallocene catalysts, nickel catalysts, or combinations of these catalysts. Catalytic systems suitable for use in the present invention have been described, for example, in US patent No. 7619047 and in applications for US patent No. 2007/0197374, 2009/0004417, 2010/0029872, 2006/0094590 and 2010/0041842, each of which is fully incorporated into the present application by reference.

[0040] In the embodiments shown in FIGS. 1-3, the polymerization of purified feed monomers may include feeding a feed stream 11 to the polymerization reactors or “reactors” 104, 106. In one or more embodiments as described herein, reactors 104, 106 may include any vessel or combination of vessels configured to provide a medium for a chemical reaction (eg, a contact zone) between monomers (eg, ethylene) and / or polymers (eg, an “active” or growing polymer chain) and, optionally, comono measures (e.g., butene-1) and / or copolymers, in the presence of a catalyst, to form a polymer (e.g., polyethylene polymer) and / or a copolymer. Although the embodiments shown in Figures 1, 2, and 3 illustrate various PES systems containing two reactors in a row, one skilled in the art will appreciate that one reactor may be used, alternatively, any suitable number and / or configuration of reactors.

[0041] As used herein, the terms “polymerization reactor” or “reactor” will include any polymerization reactor configured to polymerize olefin monomers or comonomers to form homopolymers or copolymers. Such homopolymers and copolymers are called resins or polymers. Various types of reactors include reactors that may be referred to as batch reactors, slurry reactors, gas phase reactors, solution reactors, high pressure reactors, tube reactors or autoclave reactors. Gas phase reactors may include fluidized bed reactors or multistage horizontal reactors. Suspension reactors may include horizontal or vertical loops. High pressure reactors may include autoclaves or tube reactors. Types of reactors may include batch or continuous process reactors. In continuous processes, batch or continuous discharge of the product can be used. The processes may also include partial or complete direct recycling of unreacted monomer, unreacted comonomer and / or diluent.

[0042] The polymerization reactor systems of the present invention may include one type of reactor in a system or several reactors of the same or different types. The production of polymers in several reactors may include several stages in at least two separate polymerization reactors connected by a transfer device configured to transfer the polymers obtained in the first polymerization reactor (e.g., reactor 104) to a second polymerization reactor (e.g., reactor 106 ) The required polymerization conditions in one of the reactors may differ from the operating conditions of the other reactors. Alternatively, polymerization in multiple reactors may include manually transferring the polymer from one reactor to subsequent reactors to continue polymerization. Multiple reactor systems may include any combination, including, but not limited to, several loop reactors, several gas phase reactors, a combination of loop and gas phase reactors, several high pressure reactors and / or a combination of high pressure reactors with loop and / or gas phase reactors. Several reactors can operate in series or in parallel.

[0043] According to one aspect, a polymerization reactor system may include at least one loop slurry reactor comprising vertical or horizontal loops. The monomer, diluent, catalyst, and optionally the comonomer can be continuously fed to the loop reactor in which the polymerization is carried out. 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 reactor effluent may be flash evaporated to separate the solid polymer from a liquid containing diluent, monomer and / or comonomer. Various methods can be used for this separation step, including, without limitation, flash evaporation, which may include any combination of heat input and pressure reduction; separation by cyclone in a cyclone or hydrocyclone; or separation by centrifugation.

[0044] In one or more embodiments, the comonomer may contain unsaturated hydrocarbons containing from 3 to 12 carbon atoms. For example, the comonomer may contain propene, butene-1, hexene-1, octenes, or combinations of these compounds.

[0045] A typical suspension polymerization process (also known as a particulate process) is described, for example, in US Pat. .

[0046] In some embodiments, suitable diluents used in suspension polymerization include, but are not limited to, a polymerizable monomer and, optionally, a comonomer, and hydrocarbons that are liquid under reaction conditions. Examples of suitable monomer diluents include, but are not limited to, hydrocarbons such as propane, cyclohexane, isobutane, n-butane, n-pentane, isopentane, neopentane and n-hexane. In some embodiments, 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 of these compounds. Some polymerization reactions in a loop reactor can proceed under mass polymerization conditions without the use of a diluent. An example is the polymerization of a propylene monomer as described in US Pat. No. 5,453,314, the contents of which are incorporated herein by reference in their entirety.

[0047] According to another aspect, the polymerization reactor may include at least one gas phase reactor. In such systems, 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 removed from the fluidized bed and recycled back to the reactor. At the same time, a polymer product can be taken from the reactor and a new or fresh monomer can be added to replace the polymerized monomer. Similarly, the copolymer product may optionally be removed from the reactor, and a new or fresh comonomer may be added to replace the polymerized comonomer, the polymerized monomer, or both. Such gas phase reactors may include a multi-stage gas phase polymerization of olefins, in which the olefins are polymerized in the gas phase in at least two independent gas phase polymerization zones, the polymer containing the catalyst formed in the first polymerization zone being fed into the second polymerization zone. One type of gas phase reactor is described in US patent No. 5352749, 4588790 and 5436304, the contents of each of which is fully incorporated into this application by reference.

[0048] 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 (optionally, comonomer), initiators or catalysts can be introduced. The monomer (optionally, comonomer) can be captured by a stream of inert gas and introduced into the reactor zone. Initiators, catalysts and / or catalytic components can be captured by a stream of inert gas and introduced into another zone of the reactor. Gas streams can be mixed for polymerization. Temperature and pressure can be suitably applied to obtain optimum conditions for the polymerization reaction.

[0049] According to another aspect, the polymerization reactor may include a solution polymerization reactor in which the monomer (optionally comonomer) can be contacted with the catalyst composition by suitable mixing or other means. A carrier may be used including an inert organic diluent or an excess of monomer (optionally comonomer). If desired, the monomer and / or optional comonomer in the gas phase may come into contact with the product of the catalytic reaction, in the presence or absence of a liquid material. In the polymerization zone, temperature and pressure are maintained, which lead to the formation of a polymer solution in the reaction medium.

Mixing can be used to achieve better temperature control and to maintain uniformity of the polymerization mixture throughout the polymerization zone. Appropriate means are used to divert the exothermic thermal effect of polymerization.

[0050] Polymerization reactors suitable for the described systems and methods may further include any combination of a feed system of at least one feed, at least one catalyst feed system or catalyst components, and / or at least one polymer recovery system. Suitable reactor systems may further include systems for refining raw materials, storing and preparing the catalyst, extrusion, cooling the reactor, polymer recovery, fractionation, reprocessing, storage, unloading, laboratory analysis and process control.

[0051] The conditions that are controlled to ensure the polymerization efficiency and the properties of the resin 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 molecular weight distribution. A suitable polymerization temperature may be any temperature below the depolymerization temperature according to the Gibbs free energy equation. Usually it includes a range from about 60 ° C to about 280 ° C, for example, from about 70 ° C to about 110 ° C, depending on the type of polymerization reactor.

[0052] Suitable pressures may also vary according to the type of reactor and polymerization. The pressure for liquid phase polymerization in a loop reactor is usually less than 6.89 MPa gage. (1000 psig). The pressure for gas phase polymerization is usually 1.38 to 3.45 MPa gage. (200 to 500 psig). High pressure polymerization in tubular or autoclave reactors is usually carried out at a pressure of from about 138 to 517 MPa gage. (20,000 to 75,000 psig). Polymerization reactors can also operate in the supercritical region at noticeably high temperatures and pressures. Working above the critical point of the pressure / temperature diagram (supercritical phase) can be beneficial. In one embodiment, the polymerization can take place in a medium with a suitable combination of temperature and pressure, for example, the polymerization can take place at a pressure in the range of 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 110 ° C (230 ° F), alternatively, about 91 ° C (195 ° F) to about 104 ° C (220 ° F).

[0053] You can adjust the concentration of various reagents to obtain resins with certain physical and mechanical properties. The planned final product to be obtained from the resin, and the method for producing said product, determine the required properties of the resin. Mechanical properties include tensile, bending, impact, flow, stress relaxation, and hardness tests. Physical properties include density, molecular weight, molecular weight distribution, melting point, glass transition temperature, crystal melting point, density, stereoregularity, crack growth, long chain branching, and rheological characteristics.

[0054] Concentrations and / or partial pressures of the monomer, comonomer, hydrogen, catalyst, modifiers and electron donors are important to obtain the indicated properties of the resin. Comonomers 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 to alkylate, bind poisons and control molecular weight. Modifiers can be used to control product properties, and electron donors affect stereoregularity, molecular weight distribution, or molecular weight. In addition, the concentration of poisons is minimized, since poisons affect the reactions and properties of the product.

[0055] In one embodiment, the polymerization of the monomers of the purified feed 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 reside in the first and / or second reactor 104, 106, respectively.

[0056] As described above, in the polymerization of the monomers of the purified feed, one or more polymerization reaction conditions can be selectively manipulated to obtain a given polymer product, to obtain a polymer product with one or more desired properties, to obtain the desired efficiency, to obtain the desired yield and similar results , or combinations of these results. Non-limiting examples of these parameters include pressure, temperature, type and / or amount of catalyst or cocatalyst, and concentrations and / or partial pressures of various reagents. In one embodiment, the polymerization of the monomers of the purified feedstock 52 may include adjusting one or more polymerization reaction conditions.

[0057] In one embodiment, the polymerization of the monomers of the purified feed may include providing a suitable temperature, pressure and / or partial pressure (s) during the polymerization reaction, or, alternatively, cycling between a number of suitable temperatures, pressures and / or partial pressures in during the polymerization reaction.

[0058] In one embodiment, the polymerization of the monomers of the purified feed can include circulation, flow, cyclic movement, mixing, mixing or a combination of these effects, monomers (optionally comonomers), a catalyst system and / or suspension inside and / or between the reactors 104, 106. In one embodiment, in which monomers (optionally comonomers) are circulated, a catalyst system and / or suspension, the circulation can be carried out at a speed (eg, suspension speed) of from about 1 m / s up 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.

[0059] In one embodiment, the polymerization of the monomers of the purified feed may include the configuration of reactors 104, 106 to produce a multimodal (eg, bimodal) polymer (eg, polyethylene). For example, the resulting polymer may simultaneously contain a relatively high molecular weight, low density polyethylene polymer (HMMP) and a relatively low molecular weight, high density polyethylene polymer (HMMP). For example, various types of suitable polymers may be characterized as having different densities. For example, type I may have a density in the range of from about 0.910 g / cm ³ to about 0.925 g / cm ³ , alternatively, type II may have a density of from about 0.926 g / cm ³ to about 0.940 g / cm ³ , alternatively, type III may have a density of from about 0.941 g / cm ³ to about 0.959 g / cm ³ ; alternatively, type IV may have a density above about 0.960 g / cm ³ .

[0060] In one embodiment, the polymerization of monomers may include the polymerization of comonomers in one or more polymerization reactors 104, 106.

[0061] In the embodiments shown in figures 1-3, the polymerization of the monomers of the purified feed results in a stream of polymerization products 12. Such a stream of polymerization products 12 may generally contain various solid and semi-solid substances, volatile and non-volatile liquids, gases, and combinations thereof substances. In one embodiment, the polymerization product stream 12 may comprise hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane, isobutane, pentane, hexane, hexene-1, and heavier hydrocarbons. In one embodiment, ethylene may be present in the range of from about 0.1% to about 15%, alternatively, from about 1.5% to about 5%, alternatively, from about 2% to about 4% of the total weight of the stream. Ethane may be present in the range of from about 0.001% to about 4%, alternatively, from about 0.2% to about 0.5% of the total weight of the stream. Isobutane may be present in the range of from about 80% to about 98%, alternatively, from about 92% to about 96%, alternatively, about 95% of the total mass of the stream.

[0062] Solids and / or liquids may include a polymer product (eg, a polyethylene polymer), often referred to as “polymer dust” in the PES process step. Gases may include unreacted gaseous monomer reagents or, optionally, comonomers (for example, unreacted ethylene monomers, unreacted butene-1 monomers), gaseous processed products, gaseous impurities, or combinations of these gases.

[0063] In one or more embodiments as described herein, separating the polymerization product into a polymer stream and a gas stream (eg, in block 53) may generally include removing any gases from liquids and / or solids (eg, polymer dust) using any suitable methods.

[0064] In the implementations shown in figures 1-3, the separation of the polymerization product into a polymer stream and a gas stream may include directing the stream of polymerization products 12 into the separator 108. In one or more implementations according to the present description, the separator 108 may be configured separating the stream (for example, a polymerization product containing polyethylene) into gases, liquids, solids, or combinations of these materials. The reaction product may contain unreacted gaseous monomers or, optionally, comonomers (for example, unreacted ethylene monomers, unreacted butene-1 monomers), gaseous wastes and / or gaseous impurities. As used herein, “unreacted monomer,” for example, ethylene, refers to a monomer that has been introduced into the polymerization reactor during the polymerization reaction but is not included in the polymer. As used herein, “unreacted comonomer”, for example, butene-1, refers to a comonomer that has been introduced into the polymerization reactor during the polymerization reaction but is not included in the polymer.

[0065] In one embodiment, the separator 108 may include a separator for separating the vapor from the liquid. Suitable examples of such a separator may include a distillation column, an evaporation tank, a filter, a membrane, a reactor, an absorbent, a molecular sieve, or a combination of these types. In one embodiment, the separator includes an evaporation tank. Not wishing to be bound by theory, such an evaporation tank may include a vessel configured to vaporize and / or remove components with low vapor pressure from a liquid with a high temperature and / or high pressure. The separator 108 may be configured to separate the incoming stream into a liquid stream (e.g., a condensate stream) and a gas stream (e.g., steam). The liquid stream or condensate stream may contain a reaction product (for example, polyethylene, often called "polymer dust"). The gas or vapor stream may contain volatile solvents, gaseous unreacted monomers and / or, optionally, comonomers, exhaust gases (secondary reaction products such as impurities and similar gases), or combinations of these gases. The separator may be configured to instantaneously vaporize the incoming stream by heating, reducing the pressure, or both of these methods, so that the enthalpy of the stream increases. This can be done using a heater, a pipeline heater, various other actions known in the art, or a combination of these tools. For example, a pipe heater including a double pipe may be configured to heat exchange with hot water or steam. Such a pipe heater can increase the temperature of the stream while reducing the pressure of the stream.

[0066] In one embodiment, the separation of the polymerization product into a polymer stream and a gas stream may include distillation, evaporation, flash evaporation, filtering, passing through a membrane, absorption, adsorption, or a combination of these methods, the polymerization product. In the embodiments shown in figures 1-3, the separation of the polymerization product into a polymer stream and a gas stream results in a gas stream 18 and a polymer stream 14. In one embodiment, the gas stream 18 may comprise hydrogen, nitrogen, methane, ethylene, ethane , propylene, propane, butane, isobutane, pentane, hexane, hexene-1 and heavier hydrocarbons. In one embodiment, ethylene may be present in the range of from about 0.1% to about 15%, alternatively, from about 1.5% to about 5%, alternatively, from about 2% to about 4% of the total weight of the stream. Ethane may be present in the range of from about 0.001% to about 4%, alternatively, from about 0.2% to about 0.5% of the total weight of the stream. Isobutane may be present in the range of from about 80% to about 98%, alternatively, from about 92% to about 96%, alternatively, about 95% of the total mass of the stream.

[0067] In one or more embodiments of the present disclosure, processing the polymer stream (eg, in block 54) includes any suitable method or series of methods designed to produce a polymer product that may be suitable for commercial or industrial use, storage, transportation, further processing or a combination of these applications.

[0068] In the embodiments shown in figures 1-3, processing the polymer stream may include directing the polymer stream to the processor 110. The processor 110 may be configured to implement appropriate processing means, non-limiting examples of which include cooling, injection molding, melting, granulation, blow molding, extrusion molding, rotational molding, thermoforming, injection molding and the like, or combinations thereof. Various additives and modifiers can be introduced into the polymer to ensure better processing during production and for the desired properties of the finished 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 processing aids such as waxes / oils and fluoroelastomers; and special additives, such as flame retardants, antistatic agents, absorbers, absorbents, odor improvers, and disintegrating agents.

[0069] In one embodiment, the processor 110 may be configured to form a suitable polymer product. Non-limiting examples of suitable polymeric products that can be formed by said processing include films, powders, granules, resins, liquids, or any other suitable form, as one skilled in the art will understand. Such a suitable result may be intended for use, for example, in one or more different consumer or industrial products. For example, a polymer product can be used in one or more different products, including, without limitation, bottles, barrels, toys, household containers, dishes, film products, tanks, fuel tanks, pipes, geomembranes, and facings. In a specific embodiment, the processor is configured to form granules for transporting consumer products to the manufacturer. For example, in the embodiments shown in figures 1-3, processing the polymer stream results in a polymer product 16 (e.g., granular polyethylene).

[0070] In one or more embodiments as described herein, treating a gas stream (eg, in block 57) includes any suitable method or reaction for removing oxygen, oxygen-containing compounds, oxidized compounds, or a combination of these compounds (collectively referred to as “oxygen” ) from the gas stream. Suitable methods 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 that are known to interact with oxygen, filtering, absorption, adsorption, heating, cooling, or a combination of these methods.

[0071] In the embodiments shown in FIGS. 2-3, the gas stream treatment may include directing the gas stream 18 to an oxygen removal device 118. In one or more embodiments, as described herein, an oxygen removal device 118 may include an apparatus or device, configured to remove oxygen from the gas stream. Non-limiting examples of a suitable oxygen removal device include various reactors (for example, a fluidized bed or fixed bed reactor), a filter, or a combination of these plants. A suitable oxygen removal device 118 may be configured to reduce, prevent, or prevent compounds and / or elements (e.g., oxygen) from entering the absorption reactor that may have a toxic effect on the absorption solvent (e.g., as will be described later).

[0072] In the embodiments shown in figures 2-3, processing the gas stream results in a processed gas stream 26 substantially free of oxygen. As used herein, “substantially oxygen free” refers to a flow of a fluid containing not more than 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 of the total mass flow.

[0073] In one or more embodiments of the present disclosure, separating at least one gaseous component from the gas stream and / or the treated gas stream, generally referred to as a gas stream (eg, in blocks 55, 55 or 55), generally includes any a suitable method for selectively separating 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 similar substances. In various embodiments, the gaseous component separated from the gas stream may include one or more hydrocarbons. Non-limiting examples of such hydrocarbons include alkanes (eg, butane, in particular isobutane) and alkenes or olefin monomers (eg ethylene) or, optionally, comonomers (eg, butene-1). In one embodiment, the gaseous component separated from the gas stream may comprise unreacted hydrocarbon monomer, for example, ethylene. Optionally, the gaseous component separated from the gas stream may contain unreacted hydrocarbon comonomer, for example, propene. In one embodiment, the gaseous component separated from the gas stream may comprise unreacted hydrocarbon monomer (e.g., ethylene, alone or in combination with other hydrocarbons, such as isobutane), or, optionally, a hydrocarbon comonomer (e.g., propene, alone or in combinations with other hydrocarbons such as isobutane). In one embodiment, the gaseous component separated from the gas stream may comprise ethylene, alone or in combination with isobutane. In one embodiment, the capture of isobutane can lead to cost savings in captured isobutane and a decrease in the presence of isobutane in flare emissions. Non-limiting examples of suitable separation agents include distillation, evaporation, flash evaporation, filtration, passage through a membrane, absorption, adsorption, size exclusion separation by molecular weight, size exclusion separation, polarization separation, or a combination of these methods.

[0074] In one embodiment, separating the at least one gaseous component from the gas stream may include contacting the gas stream with an absorbent (eg, an absorbent solvent system, as will be described later), for example, to allow absorption of the gaseous component by an absorbent. In said embodiment, separating the at least one gaseous component from the gas stream comprises selectively absorbing the at least one gaseous component from the gas stream. In said embodiment, 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, allowing at least one gaseous component to be absorbed by the absorbent, and optionally removing an exhaust stream containing non-absorbed gases. In a further embodiment, separating the at least one gaseous component from the gas stream may further include separating the absorbed gaseous component from the absorbent.

[0075] In one embodiment, bringing the gas stream into contact with the absorbent may include any suitable means of providing sufficient contact between the gas stream and the absorbent. Non-limiting examples of suitable means to ensure sufficient contact between the gas stream and the absorbent include the use of various reactor systems, including the systems described above (for example, an absorption column or bubbler or mixing tank). Without wishing to be bound by theory, a suitable reactor system can provide contact between two or more gaseous, liquid and / or solid compositions by mixing or mixing the two compositions in the presence of each other, circulating, dispersing or diffusing the first composition through or inside the second composition, or various other techniques known to those skilled in the art. In one embodiment, the gas stream and the absorbent can be contacted in an appropriate manner. This suitable gas flow to absorbent ratio can range from about 454 kg / h: 3,785 l / min (1,000 lb / hr: 1,000 gpm) to about 1,134 kg / h: 95 l / min (2,500 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).

[0076] In the embodiment shown in figures 1-3, the separation of at least one gaseous component from the gas stream (for example, the gas stream 18 in figure 1 or the processed gas stream 26 in figures 2-3) may include a direction of gas flow in absorption reactor 116. In one or more embodiments, as described herein, absorption reactor 116 may include a reactor configured to selectively absorb at least a first chemical component or compound from a stream containing the first chemistries esky component or compound and one or more other chemical components, such compounds or substances. Non-limiting examples of suitable configurations of absorption reactors and / or adsorption reactors include an absorption tower, a differential pressure absorption (APD) configuration, an irrigation tank, a stirred reactor, one or more compressors, one or more recirculation pumps, or combinations of these configurations.

[0077] In one embodiment, the absorption reactor may be configured to disperse gas in a liquid (for example, by sparging gas through a liquid). For example, in one embodiment, the absorption reactor 116 may include a solvent circulation system configured to circulate the solvent through the absorption reactor 116. The solvent circulation rate may be determined by the operating conditions of the absorption system, as described below. In one embodiment, the absorption reactor 116 may include and / or in fluid communication with one or more pumps configured to recycle the solvent through and / or inside the absorption reactor 116. In a further and / or alternative embodiment, the absorption reactor 116 may include a packing layer or column configured to provide small bubble sizes (e.g., gas scattered in the liquid), for example, so as to provide a relatively large surface contact between the gas and the liquid, e.g., so as to ensure the effectiveness of the mass transfer and / or removal of gas in the liquid. In one embodiment, the packing material of the packing of the packing or column may include a polymeric material, a metallic material, or a combination of these materials. In one embodiment, the absorption reactor 116 may include multiple layers of packing or columns. In one embodiment, only a portion of the absorption reactor 116 may comprise packing material. In one embodiment, the material of the packing of the absorption reactor 116 with the packing may be randomly packed or have a structured packing. An example of a suitable absorption reactor is shown in the Gas Processors Association, Engineering Data Book 10th ed. in FIG. 19-16.

[0078] In an embodiment in which the absorption reactor 116 includes a solution reactor, said absorption reactor may include a suitable system of absorption solvents, as will be described below. Such an absorption reactor 116 may be configured to retain an absorbent solvent system. For example, an absorbent solvent system can be held in the reactor as a liquid, as a fixed bed, or as a fluidized bed.

[0079] In one embodiment, a suitable absorbent solvent system may be capable of reversibly complexing with ethylene and / or isobutane. Such an absorbent solvent system may generally comprise a complexing agent and a solvent. In one embodiment, an absorbent solvent system can be characterized in that it is ethylene selective compared to ethane if ethylene and ethane are present at the same partial pressure of about 40: 1 at a partial pressure of about 97 kPa (14 psi), about 12 : 1 at about 138 kPa (20 psi), about 6: 1 at about 276 kPa (40 psi), and about 3: 1 at about 1.24 MPa (180 psi). In one embodiment, the solvent system may additionally be characterized by high tolerance to contaminants and high stability at elevated and / or variable temperatures and / or pressures, or a combination of these properties.

[0080] In one embodiment, the complexing agent may comprise a metal salt. In such an embodiment, 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. In one embodiment, a suitable transition metal salt may be highly specific for olefins. Non-limiting examples of suitable transition metal and halogen salts include silver chloride (AgCl) and copper chloride (CuCl). In a specific embodiment, the salt used in the absorbent solvent system includes CuCl. Not wanting to be bound by theory, said metal salt can interact with a carbon-carbon double bond in olefins (e.g., ethylene).

[0081] In one embodiment, the complexing agent may include copper (I) carboxylate. In this embodiment, suitable copper (I) carboxylates may include salts of copper (I) and mono-, di- and / or tricarboxylic acids containing 1-20 carbon atoms. The carboxylic acid component of the salt may include an aliphatic moiety, a cyclic moiety, an aryl moiety, or combinations of these moieties. 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-ethylhexanoate, Cu (I) hexadecanoate, Cu (I) tetradecanoate, Cu (I) methyl formate, Cu (I) ethyl acetate, Cu (I) n-propyl acetate, n-butyl acetate Cu (I), ethyl propanoate Cu (I), octoate Cu (I), benzoate Cu (I), para-tert-butyl benzoate Cu (I) and the like salts. In further embodiments, the complexing agent may include an adduct of copper (I) carboxylate, for example, as described herein, and boron trifluoride (BF ₃ ).

[0082] In a further and / or alternative embodiment, the complexing agent may include 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 the salt may include an aliphatic moiety, a cyclic moiety, an aryl moiety, or combinations of these moieties. 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, dodecansulfonic acid, 2-ethyl-5-n-pentyltridecanesulfonic acid, n-eicosansulfonic acids . Examples of suitable aromatic sulfonic acids include benzenesulfonic acid, alkylbenzenesulfonic acids, where the alkyl moiety contains from 1 to 16 carbon atoms, such as para-toluenesulfonic acid, dodecylbenzenesulfonic acid (ortho-, meta- and para-), para-hexadecylbenzenesulfonic acid, and acids, naphthalenesulfonic acid, phenolsulfonic acid, naphtholsulfonic acids and halogenbenzenesulfonic acids such as para-chlorobenzenesulfonic acid, para-bromobenzenesulfonic acid a and like acids.

[0083] In one embodiment, the complexing agent may further comprise a hindered olefin. For example, the complexing agent may contain such a difficult olefin in an embodiment 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, while being easily replaced by ethylene.

[0084] In various embodiments, the complexing agent may include one or more complexing agents described in US patent No. 5104570; 5,191,153; 5,259,986; and 5523512, each of which is fully incorporated into this application by reference.

[0085] In one embodiment, the solvent may include an amine or amine complex, an aromatic hydrocarbon, an olefin, or a combination of these solvents. Non-limiting examples of amine solvents include pyridine, benzylamine, and aniline. For example, an amine may include aniline (phenylamine, aminobenzene); alternatively, aniline in combination with dimethylformamide (DMF), and in some of the embodiments, aniline and N-methylpyrrolidone (NMP). In embodiments where the solvent is an aromatic hydrocarbon, said aromatic hydrocarbon may contain unsubstituted or alkyl substituted aryl groups. In such an embodiment, the aromatic hydrocarbon may be liquid under normal environmental conditions. Suitable non-limiting examples include toluene, xylene, and the like. In those embodiments where the solvent includes an olefin, non-limiting examples include olefins containing from 10 to 16 carbon atoms. For example, the olefin may include propylene tetramer, dodecene, tetradecene, hexadecene, or combinations of these compounds.

[0086] In one embodiment, the solvent may be characterized as aprotic, that is, not containing dissociable hydrogen atoms. Without wishing to be bound by theory, a solvent capable of dissociating 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, weakly polar or having a unidirectional electric charge. Without wishing to be bound by theory, the polar solvent can interact with the salt and at least partially solubilize the salt.

[0087] In one embodiment, the solvent can be characterized as a liquid obtained industrially in relatively large volumes, having a relatively low cost, relatively easily transported, or having a combination of these properties. The solvent may be further characterized as being capable of retaining the olefin-metal salt complex or preserving the weakly ionic metal salt, despite fluctuations in temperature and / or pressure.

[0088] In one embodiment, 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). In such an embodiment, the CuCl / aniline / NMP solvent system may be characterized by increased volatility stability 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. In alternative embodiments, the absorbent solvent system may include the adduct of copper (I) carboxylate and BF ₃ in an aromatic solvent such as toluene or xylene.

[0089] In one embodiment, the absorbent solvent system may comprise copper (I) 2-ethylhexanoate and propylene tetramer. In one embodiment, the absorbent solvent system may comprise copper (I) 2-ethylhexanoate 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.

[0090] In one embodiment, enabling the at least one component to be absorbed by the absorbent includes enabling the at least one component to form a reversible bond, compound or binding, or a combination of these bonds, with the absorbent or with a portion of the absorbent, for example, the formation of various bonds, affinities, complexes or combinations of these interactions. For example, in an embodiment in which the absorbent comprises an absorbent solvent system (for example, a CuCl / aniline / DMF solvent system or a CuCl / aniline / NMP solvent system), allowing absorption of at least one component may include allowing complex formation between the absorbent and at least one component called an absorbed component complex (e.g., an absorbed ethylene complex).

[0091] Enabling the absorption of at least one component may further include providing and / or maintaining a suitable ambient pressure at which the gas stream and absorbent come into contact, providing and / or maintaining a suitable partial gas pressure, providing and / or maintaining a suitable the ambient temperature at which the gas stream and the absorbent come into contact, the implementation of catalysis of absorption or a combination of these methods. Without wishing to be bound by theory, the absorption of at least one component can be improved at a suitable temperature and / or pressure.

[0092] In one embodiment, the absorption reactor 116 may be configured to selectively induce fluctuations, changes or cycles of 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 optionally comonomer) from a composition containing various other gases (e.g., ethane). In another embodiment, 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 another embodiment, the absorption reactor 116 may be configured to selectively absorb simultaneously unreacted ethylene and butane, in particular isobutane, from a composition containing various other gases (e.g. ethane).

[0093] In one embodiment, the absorption reactor 116 may be configured to provide or maintain a suitable temperature, for example, depending 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, to increase the absorption of the desired chemical compounds, reduce the absorption of the desired chemical compounds, instantly evaporate unabsorbed gas from the reactor 116, extract unreacted ethylene from the absorption reactor 116, and regenerate the absorbent in an absorption reactor 116 or combinations of these purposes. In one embodiment, such a suitable temperature may range from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), alternatively from about 4 ° C (40 ° F) to about 16 ° C. (60 ° F), alternatively, from about 7 ° 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 the system of absorbent solvents), which is in the temperature range from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), alternatively, from about 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 compared to ethane absorption. Not wanting to be bound by theory, a person skilled in the art will understand (for example, based on the concept of partial pressure according to Raoult's law) that an increase in the solubility of ethylene and ethane in an absorbing solvent is expected at lower temperatures. However, contrary to these expectations, it was found that the amount of ethylene absorbed by the absorbent solvent and / or the system of absorbent solvents according to the embodiments of the present invention decreases with decreasing temperatures below 10 ° C (50 ° F). Due to this unexpected phenomenon, ethylene absorption may be greatest for temperatures ranging from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), alternatively, in the range from about 4 ° C (40 ° F) to about 16 ° C (60 ° F), alternatively, at a temperature of about 10 ° C (50 ° F). Figure 7 is a graph showing the solubility at various temperatures of ethylene and ethane in an absorbent solvent system of copper chloride, aniline, NMP. The graph illustrates the expected ethane solubility curve and the unexpected ethylene solubility curve in the temperature range discussed above.

[0094] In one embodiment, the absorption reactor 116 may be configured to provide or maintain a suitable temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F) during the absorption of one or more components gas stream (e.g. ethylene and / or isobutane). As described above, it was found that the solubility of ethylene is unexpectedly greatest at temperatures ranging from about 4 ° C (40 ° F) to about 16 ° C (60 ° F). In one embodiment, the absorption reactor 116 may operate at a temperature of from about 4 ° C (40 ° F) to about 16 ° C (60 ° F), alternatively, at a temperature of about 10 ° C (50 ° F) during the absorption of ethylene and / or isobutene from the gas stream. In an alternative embodiment, the absorption reactor may be operated 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) during the absorption of ethylene and / or isobutene from the gas stream. For example, such absorption temperatures in the absorption reactor 116 may be suitable as an economical 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 can lead to cost savings by allowing the reactor to operate at ambient temperature in a given geographic location.

[0095] In one embodiment, the absorption reactor 116 may be configured to provide or maintain a suitable pressure during operation. Such a suitable pressure may range from about 34 kPa gage. (5 psig) to about 3.45 MPa gage. (500 psig), alternatively, from about 345 kPa gage. (50 psig) to about 3.10 MPa gage. (450 psig), alternatively, from about 517 kPa gage. (75 psig) to about 2.76 MPa gage. (400 psig). In a further embodiment, 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 range from about 7 kPa abs. (1 psia) to about 2.76 MPa 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 517 kPa abs. (75 psia), alternatively, from about 276 kPa gage. (40 psig) to about 414 kPa (60 psig), alternatively, about 276 kPa gage. (40 psig), alternatively, about 414 kPa gage. (60 psig). Without delving into theory, providing pressure in the absorption reactor 116 may facilitate the absorption of ethylene and / or the formation of a complex of ethylene and an absorbent solvent system (e.g., CuCl / aniline / NMP system). Also, without delving into theory, the selectivity of the system of absorbent solvents to ethylene can increase with decreasing pressure in the absorption reactor.

[0096] In one embodiment, the absorption reactor 116 may be configured to intermittently and / or continuously. For example, in one embodiment, the PES system may include two or more absorption reactors (for example, such as absorption reactor 116), each of which may be batch capable. For example, through the use of two or more absorption reactors, the system can be made to continuously operate by absorbing a gas stream component into a “first batch” in a first absorption reactor, while a “second batch” is prepared for absorption in a second absorption reactor. Thus, by cyclic switching between two or more suitable reactors, the system can operate continuously.

[0097] For example, in one embodiment, two or more absorption reactors (eg, a system of absorption reactors) can be configured to adsorb ethylene differential pressure (APD) using a liquid solvent, for example, an absorbent solvent system or an absorbent solvent according to the present description. In such an embodiment, the absorption reactor 116 may include two or more absorption reactors configured for APD (for example, an absorption reactor system). The figure 8 shows a system of absorption reactors 800 with four absorption reactors 810, 820, 830 and 840, made with the possibility of APD. Although in the embodiment of FIG. 8, four absorption reactors are shown (for example, absorption reactors 810, 820, 830 and 840), one skilled in the art, when considering the present description, will understand that two, three, five, six, seven, eight or more absorption reactors. In such an embodiment, each of the absorption reactors can be made essentially as described in this application. In one embodiment, one or more reactors 810, 820, 830, and 840 may be connected by a circulation system (for example, including one or more pumps, valves, pipelines, and the like) to circulate a liquid solvent in reactors 810, 820, 830, and 840 during absorption. Absorption reactors 810, 820, 830, and 840 can act cyclically 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 included in the composition of the complex, the gaseous component is released from the system of absorbent solvents and / or the system of absorbent solvents is prepared for reuse, as will be described below). For example, reactors 810, 820, 830, and 840 can act cyclically between the phases of absorption and regeneration (for example, through one or more intermediate phases) in a coordinated mode, so that not all reactors 810, 820, 830, 840 undergo absorption or regeneration at the same time. In an embodiment in which the absorption reactors 810, 820, 830 and 840 are configured to operate in the ADF, the reactors 810, 820, 830 and 840 serve as absorbers and regenerators. In such an embodiment, separate vessels for regeneration may not be required (for example, as described herein).

[0098] As an example of operation in the ADF in a consistent mode, in this phase during this operation, the reactor 810 can act on the absorption phase, for example, under absorption conditions as described herein. Essentially at the same time, an intermediate pressure can be injected into the reactor 820, for example, below the absorption pressure. Also, essentially at the same time, it is possible to reduce the pressure from the intermediate pressure to the regeneration pressure in the reactor 830, while the pressure from the absorption pressure (from the previous absorption phase) to the intermediate pressure can be reduced in the reactor 840. Not wanting to be bound by theory, pressure reduction (for example, from absorption pressure to intermediate pressure and from intermediate pressure to regeneration pressure) in each of the reactors 810, 820, 830 and / or 840 after absorption can provide the possibility of the release of gaseous components (for example, ethylene and / or isobutane) from the absorbent and / or regeneration of the absorbent (for example, preparation for repeated use, as described herein). In one embodiment, the pressure from one or more reactors (e.g., reactors 810, 820, 830 and / or 840) can be used to increase the pressure in another of these reactors. For example, in the embodiment of FIG. 8, the gas pressure in reactor 840 can be used to increase the pressure in reactor 820 to an intermediate pressure through line 850 with valves 858 and 884 in the open position and valves 882 and 856 in the closed position. Valves 862, 864, 866, and 868 can be switched between open position and closed position to allow nitrogen product in stream 860 to flow into and out of reactors 810, 820, 830, and 840. Valves 852, 854, 856, and 858 can be switched between open position and a closed position to allow for pressure increase and pressure reduction in reactors 810, 820, 830 and 840 through flow 850. Valves 882, 884, 886 and 888 can be switched between open position and closed position to allow light gases 880 to flow into reactors 810, 820, 830 and 840 in the absorption phase. Valves 892, 894, 896, and 898 can be switched between an open position and a closed position to remove any purge gas from reactors 810, 820, 830, and 840 via flow 890.

[0099] In one embodiment, a stripping gas, such as isobutane or nitrogen, can be introduced into the absorption reactors 810, 820, 830 and 840, for example, via stream 870 during the regeneration phase. Stream 870 can be located at the bottom of reactors 810, 820, 830 and 840 so that the stripping gas can sparge through reactor 810, 820, 830 or 840 (and through any packing material therein). Valves 872, 874, 876, and 878 can be switched between an open position and a closed position for supplying stripping gas to reactors 810, 820, 830, and 840 during regeneration. Not wanting to be bound by theory, the stripping gas can lower the partial pressure of ethylene in absorption reactors 810, 820, 830 and 840 during regeneration.

[00100] In one embodiment, one or more absorption reactors 810, 820, 830, and 840 may include internal elements to distribute gas in a liquid absorbent solvent and prevent channel formation. Suitable internal elements may include a distillation nozzle that distributes gas and reduces axial mixing of the liquid. The internal elements can prevent mixing of the liquid absorption solvent in the absorption reactors 810, 820, 830 and 840, so that the solvent flow first reaches saturation, and then the saturated front can advance vertically through the absorption reactors 810, 820, 830 and 840.

[00101] In one embodiment, separating the at least one component from the gas stream includes removing the waste stream. In one embodiment, the remaining non-absorbed components of the gas stream form an exhaust stream. In one embodiment, in which the absorbed components contain ethylene and the absorbent contains a solvent system CuCl / aniline / DMF or CuCl / aniline / NMP, such a waste stream may contain methane, ethane, acetylene, propylene, various other hydrocarbons, volatile impurities or combinations of these gases. In addition, such a spent stream may essentially not contain unreacted ethylene monomers and, optionally, comonomers. As used herein, “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% of unreacted ethylene monomers, alternatively, less than 0.01% of unreacted ethylene monomers, based on the total weight of the stream.

[00102] In one embodiment, the removal of the waste stream may include cooling the waste stream and / or lowering or increasing the pressure of the waste stream so that the waste stream enters the processing device 114. For example, in one embodiment, the waste stream may be “discarded” by supplying a suitable purge gas (e.g., an inert or inactive gas, as described above) through a vessel containing exhaust gas (e.g., absorption reactor 116), with sufficient pressure, speed, or com Inácio said parameters for removing exhaust gases from said vessel. For example, in the embodiments shown in figures 1-3, separating at least one component from the stream results in an exhaust gas stream 20 substantially free of unreacted ethylene monomers (optionally comonomers), alternatively, a reduced concentration of exhaust gas unreacted ethylene monomers (optionally comonomers). For example, the exhaust gas stream may contain less than about 30%, alternatively, less than about 25%, alternatively, less than about 20%, alternatively, less than about 15%, alternatively, less than about 10% of unreacted ethylene monomers of the total mass of the stream. In a further embodiment, the content of ethylene present in the gas stream before separation of the at least one gaseous component from said stream can be reduced by a certain percentage of ethylene. For example, the exhaust gas stream may contain less than about 40%, alternatively, less than about 30%, alternatively, less than about 20% of the total mass of the stream, unreacted ethylene monomers present in the gas stream before separation.

[00103] In one embodiment, separating the at least one component from the gas stream may further include releasing the absorbed gaseous component from the absorbent (for example, in situ in the 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 reversing various bonds, affinities, complexes or combinations of these interactions, by which at least one gaseous component forms a compound, bond, or combinations thereof with an absorbent or part of the absorbent. Non-limiting examples of suitable means by which the absorbed gaseous component is released include changing the kinetics of absorption or absorption equilibrium in the absorbent, heating or lowering the pressure of the absorbent, changing the partial pressure of the absorbed gas, or a combination of these.

[00104] In one embodiment, the absorbed gaseous component can be released (for example, to desorb and / or destroy the complex) from the absorbent within one or more of these absorption reactors in the regeneration and / or desorption phase. For example, in the embodiment shown in figures 1 and 2 (and / or in the embodiment in which the absorption reactor 116 is configured to configure the ADF, as described in this application with reference to figure 8), the absorption reactor 116 may be made with the ability to induce the release of gas absorbed or complexed with an absorbent solvent from said solvent (e.g., desorption and / or destruction of a complex of absorbed and / or complexed ethylene and / or isobutane), as an fully described in this application. Without wishing to be bound by theory, inducing the release of absorbed or complexed gas may include changing the kinetics of the reaction or the equilibrium between the gas and the solvent in the system of absorbing solvents, the temperature of the absorption reactor 116, the pressure in the absorption reactor 116, the partial pressure of the absorbed gas, or a combination of these parameters. In such an embodiment, the absorption reactor 116 may include controls, thermal conductors, electrical conductors, compressors, vacuum devices, and the like, or combinations of these devices configured to alter the reaction kinetics, equilibrium between gas and solvent, temperature of the absorption reactor 116, pressure in the absorption reactor 116 or a combination of these parameters.

[00105] For example, in one embodiment, the release of the absorbed gaseous component may include reducing the pressure over the solution containing the complexed ethylene to a suitable partial pressure. In an additional embodiment, the release of the absorbed gaseous component may include heating the solution containing the complexed ethylene in the absorption reactor 116 (alternatively, in the regenerator 120, as described below), to a suitable temperature. Such a suitable temperature may range 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) to cause release an 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 isobutane) from the absorbent solvent. In an alternative embodiment, 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 isobutane ) from an absorbent solvent. For example, such a release temperature may be suitable as an economic alternative. For example, operating 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 release of the absorbed a component may require less energy, which can lead to cost savings by providing the possibility of obtaining heat from other sources (for example, a cooler of a polymerization reactor, low pressure steam, heat exchangers upstream of the regen to heaters in absorbent recirculation lines, polymerization reactors, flash heaters, flash vessels and similar sources, or combinations of these sources) for use in heating an absorption reactor and / or regenerator.

[00106] Furthermore, in such an embodiment, 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 the absorbed gas by means of differential pressure. The absorption reactor 116 may be configured to provide or maintain a suitable partial pressure. Such a suitable partial pressure may be in the range of 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 34kPa huts. (5 psig) to about 103 kPa (15 psig). In one embodiment, the absorption reactor 116 may be configured to provide or maintain a partial ethylene pressure in the range of about 0 kPa abs. (0 psia) to about 34 kPa abs. (5 psia).

[00107] In an alternative embodiment, separating at least one component from the gas stream may further include removing a solution containing the absorbed complex of the component (eg, the absorbed ethylene complex) for further processing. In such an alternative embodiment, the absorption complex containing the absorbed gaseous component can be removed from the absorption reactor 116 to a regenerator 120 to release the absorbed gaseous component and / or regenerate the absorption complex as a complex stream 28. In such an embodiment, the complex stream 28 may contain ethylene ethane and / or isobutane. Ethylene may be present in the range 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% of the total weight of the stream. Ethane may be present in the range of from about 0.1% to about 1%, alternatively, from about 0.2% to about 0.5% of the total weight of the stream. Isobutane may be present in the range of from about 0.1% to about 1%, alternatively, from about 0.2% to about 0.5% of the total weight of the stream.

[00108] In one or more embodiments as described herein, separating the complex stream into a recycle stream and an absorbent stream (for example, at block 58) includes releasing the absorbed gaseous component from the absorbent. As described above, the release of the absorbed gaseous component from the absorbent as a whole includes any suitable means of reversing the various bonds, attractiveness, complexes or combinations of these interactions by which at least one gaseous component forms a compound, bond or combination thereof with the absorbent or part thereof. Various methods and parameters for the release of the absorbed gaseous component have been described above when considering the release in the absorption reactor.

[00109] In the embodiment shown in FIG. 3, separating the complex stream into a recycle stream and the absorbent stream may include directing the complex stream 28 to the regenerator 120. In one or more embodiments of the present disclosure, the regenerator 120 may include a device or installation configured to the ability to recover, regenerate, recycle and / or purify the absorbent solvent and / or release the absorbed gas. Non-limiting examples of a suitable regenerator include a flash reactor, a pressure reduction reactor, a solvent recovery reactor, or a combination of these reactors.

[00110] In one embodiment, the regenerator 120 may be configured to operate due to a pressure difference. In such an embodiment, the regenerator 120 may be configured to provide or maintain a suitable internal pressure. Such a suitable internal pressure may range from about 0 kPa gage. (0 psig) to about 1.03 MPa gage. (150 psig), alternatively, from about 34 kPa gage. (5 psig) to about 207 kPa (30 psig), alternatively, from about 34kPa huts. (5 psig) to about 103 kPa (15 psig), alternatively, from about 0 kPa 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 in the range of about 0 kPa abs. (0 psia) to about 345 kPa abs. (50 psia).

[00111] In one embodiment, the regenerator 120 may be configured to operate due to elevated temperature. Such a regenerator 120 may be configured to provide or maintain a suitable temperature. Such a suitable temperature may range 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), to vaporize and / or release the absorbed compound (e.g., ethylene and / or isobutane) from the absorbent solvent. In one embodiment, the regenerator 120 (for example, similarly to the absorption reactor 116) can be heated to desorb or regenerate the system of absorbent solvents using heat sources including cooling water, low pressure steam, or a combination of these. Cooling water, low pressure steam, or a combination of these 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).

[00112] In one embodiment, the regenerator 120 may be configured to intermittently and / or continuously. For example, in one embodiment, the PES system may include two or more absorption regenerators (eg, such as regenerator 120), each of which may be configured to intermittently. As described above, through the use of two or more absorption regenerators, the system can operate with continuous regeneration of the absorbent.

[00113] In one embodiment, the separation of the complex stream into a recycle stream and an absorbent stream results in a regenerated absorbent stream that can be reused in the absorption reaction, and a recycle stream including unreacted monomers (optionally comonomers) that can be reintroduced or reapplied in the PES method. For example, in the embodiment shown in FIG. 3, separation of the complex stream into a recycle stream and an absorbent stream 58 results in a recycle stream 22 that can be returned to the purifier 102 and a regenerated absorbent stream 30 that can be returned to the absorption reactor 116 .

[00114] In one embodiment, the release of absorbed gas also results in a recycle stream containing unreacted monomers (optionally comonomers) that can be returned to the separator 108 for compression (for example, using one or more compressors located in the separator 108 ) For example, in the embodiments shown in figures 1-3, the release of absorbed gas results in a recycle stream 22, which can be returned to the separator 108. Compression of the recycle stream 22 results in a re-stream 24, which can be re-introduced or reused in the PES method. For example, in the embodiments shown in figures 1-3, the re-introduced stream 24 is introduced into the purifier 102. In an alternative embodiment, the recycled stream (such as the recycled stream 22) can be compressed and / or re-introduced into the PES method without returning to the separator 108. In one embodiment, recycled stream 22 may comprise substantially pure ethylene; alternatively, recycle stream 22 may comprise ethylene and butane, in particular isobutane. In one embodiment, the gas stream may comprise nitrogen, ethylene, ethane and / or isobutane. Ethylene may be present in the range of from about 65% to about 99%, alternatively, from about 70% to about 90%, alternatively, from about 75% to about 85% of the total weight of the stream. Ethane may be present in the range of from about 1% to about 20%, alternatively, from about 5% to about 15%, alternatively, from about 7.5% to about 12.5% of the total weight of the stream. Isobutane may be present in the range of from about 1% to about 20%, alternatively, from about 5% to about 15%, alternatively, from about 7.5% to about 12.5% of the total weight of the stream.

[00115] In one or more embodiments of the present description, burning an exhaust gas stream (eg, in block 56) may generally include burning or burning one or more gaseous components of the exhaust gas stream 20. In one or more embodiments of the present description, burning exhaust gas stream 20 may additionally or alternatively include cracking, catalytic cracking, pyrolysis, dehydrogenation, scrubbing, converting, processing or combinations of these tvy, the flow of exhaust gases 20 or the combustion products.

[00116] According to the present description, the exhaust gas stream 20 may include evaporated solvents, unreacted gases, secondary products, impurities, hydrocarbons, or combinations of these gases. In one embodiment, the exhaust gas stream 20 may comprise hydrogen, nitrogen, methane, ethylene, ethane, propylene, propane, butane, isobutane, heavier hydrocarbons, or combinations of these compounds. Ethylene may be present in the range of from about 1% to about 40%, alternatively, from about 2.5% to about 20% of the total weight of the stream. Ethane may be present in the range of from about 5% to about 50%, alternatively, from about 30% to about 40% of the total weight of the stream. Isobutane may be present in the range of from about 1% to about 20%, alternatively, from about 1.5% to about 5%, alternatively, from about 2% to about 3% of the total weight of the stream. Nitrogen may be present in the range of from about 10% to about 80%, alternatively, from about 35% to about 50%, alternatively, from about 40% to about 45% of the total mass of the stream.

[00117] In the embodiments shown in FIGS. 1-3, burning the exhaust gas stream includes directing the exhaust gas stream 20 to the processing device 114. In one or more embodiments of the present disclosure, the processing device 114 may include a combustion unit or device, such like a torch. Non-limiting examples of a suitable torch include a burner, incinerator, and similar devices, or combinations of these devices. The torch may include one or more controlled nozzles, an ignition source, a bypass valve, a pressure relief valve, or a combination of these elements. The torch may 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 of these gases. In one embodiment, the flare may further include an installation or device configured to selectively remove one or more impurities before, during, and / or after combustion (for example, so that a given combustion product does not enter the atmosphere).

[00118] In one or more embodiments of the present disclosure, the processing device 114 may include, for example, a cracking device, a catalytic cracking device, a scrubber, a converter, a processing device, a dehydrogenation device, an oxygen removal device, or combinations of these devices. In one embodiment, the processing device 114 may include an ethylene cracker. In the 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 the processing device 114, for example, can be returned to one or more of the following devices: purifier 102, reactor 104, reactor 106.

[00119] In other alternative embodiments, the exhaust gas stream 20 can be used as fuel (for example, to generate steam or operate a CHP) and / or can be used as fuel and / or raw material for a thermal cracking unit to produce ethylene (for example, to produce flow of raw materials 10). In another alternative embodiment, the exhaust gas from the exhaust gas stream 20 can be sent from plant to plant to produce monomer.

[00120] In one embodiment, the implementation of one or more of the described systems (eg, PES systems 100, 200 and / or 300) and / or methods (eg, PES methods 400, 500 and / or 600) allows the extraction of a significant portion ethylene monomers that would otherwise be lost due to the operation of such systems or methods, for example, by flaring. In one embodiment, one or more systems as described herein can recover up to about 75%, alternatively, about 85%, alternatively, about 90%, alternatively, about 95% of the total weight of the ethylene monomer stream that would otherwise be lost . In one embodiment, one or more of the systems described herein allows recovery of up to about 75%, alternatively, about 85%, alternatively, about 90%, alternatively, about 95% of the total mass of the isobutane stream that would otherwise be lost. The extraction of such a portion of unreacted ethylene monomers can lead to significant economic benefits, for example, due to increased efficiency in the use of ethylene monomers and lower capital investments associated with the acquisition of ethylene monomers. Similarly, the recovery of such a portion of isobutane can lead to significant economic benefits, for example, due to a reduction in capital investments associated with the acquisition of isobutane and / or due to a decrease in the isobutane content in flare emissions.

[00121] In one embodiment, the implementation of one or more systems and / or methods as described herein can reduce the amount of ethane 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 returned to the polymerization reactor, the overall efficiency of producing polyethylene can be improved (for example, by increasing the ethylene concentration without reaching the boiling point in the loop reactor). For example, reducing the amount of ethane in the recycle stream can increase the efficiency of the polymerization reactor, increase the efficiency of the catalyst, reduce polymer contamination, reduce downtime during polymerization or cause a combination of these effects.

[00122] A person skilled in the art will understand that industrial and commercial methods for producing polyethylene may require one or more, often several, compressors or similar installations. Such compressors are used in the production of polyethylene, for example, to create pressure in reactors 104, 106 during polymerization. In addition, an experienced specialist in the art will understand that the method of producing polyethylene includes one or more devices for removing oxygen and / or similar plants for removing oxygen, for example, for cleaning solvents or reagents and / or for purging reactors from oxygen. Since the infrastructure and provision of these facilities, for example, for supplying energy and servicing compressors and / or oxygen removal devices, already exists in a commercial polyethylene production plant, redirecting some of these available resources for use in systems according to the present description may require a little if generally require additional investment to include systems and / or methods as described herein.

[00123] In addition, since compressors, oxygen removal devices, and various other components are already used in various methods and systems for producing polyethylene, the possibility of improved operation of such plants can increase the overall efficiency of systems and methods for producing polyethylene. For example, when part of the PES method or system is disconnected from the line for maintenance and / or repair, other parts of the system (eg, compressor, oxygen removal device, reactor, etc.) may continue to provide service according to current methods. The resources of operation and / or redistribution for the operation of systems and / or PES methods according to the present description can, therefore, increase the efficiency of using traditional systems.

ADDITIONAL DESCRIPTION

[00124] A method and system for producing polyethylene have been described. The following points are taken as an additional description:

[00125] Embodiment A. A method for extracting ethylene from a polymerization product stream of a polyethylene production system, comprising:

separating the light gas stream from the polymerization product stream, said light gas stream containing ethane and unreacted ethylene;

bringing into contact the light gas stream with a system of absorbent solvents, wherein said contacting a stream of light gases with a system of absorbent solvents occurs at a temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), wherein at least a portion of the unreacted ethylene from the light gas stream is absorbed by an absorbent solvent system; and

recovering unreacted ethylene from an absorbent solvent system to produce recovered ethylene.

[00126] Embodiment B. The method of claim 1, wherein the absorbent solvent system comprises copper chloride, aniline, and N-methylpyrrolidone.

[00127] Embodiment C. The method of claim 1, wherein contacting the light gas stream with a system of absorbent solvents occurs at a temperature in the range of from about 4 ° C (40 ° F) to about 16 ° C (60 ° F).

[00128] Embodiment D. The method of claim 3, wherein contacting the light gas stream with a system of absorbent solvents occurs at a temperature of about 10 ° C (50 ° F).

[00129] Embodiment E. The method of claim 1, wherein contacting the light gas stream with a system of absorbent solvents occurs at a temperature in the range of from about 16 ° C (60 ° F) to about 32 ° C (90 ° F).

[00130] Embodiment F. The method of claim 5, further comprising:

introducing stripping gas into the absorbent solvent system, wherein at least a portion of said stripping gas is absorbed by the absorbent solvent system.

[00131] Embodiment G. The method of claim 6, wherein said stripping gas is selected from the group consisting of nitrogen and isobutane.

[00132] Embodiment H. The method of claim 1, wherein contacting the light gas stream with a system of absorbent solvents comprises sparging a stream of light gas through a nozzle layer in a system of absorbent solvents.

[00133] Embodiment I. The method of claim 1, wherein contacting the light gas stream with the absorbent solvent system comprises increasing the pressure of the light gas stream and the absorbent solvent system to a pressure in the range of about 40 psi. inch hut up to about 60 psi inch hut

[00134] Embodiment J. The method of claim 1, wherein recovering the unreacted ethylene from the absorbent solvent system comprises lowering the pressure of the absorbent solvent system with absorbed unreacted ethylene at a temperature in the range of from about 43 ° C (110 ° F) to about 93 ° C (200 ° F).

[00135] An implementation option K. The method according to p. 10, characterized in that the pressure reduction of the system of absorbent solvents occurs at a pressure in the range from about 0 kPa gage. (0 psig). up to about 69 kPa (10 psig).

[00136] An implementation option L. The method according to p. 10, characterized in that the pressure reduction of the system of absorbent solvents with absorbed unreacted ethylene occurs at a temperature in the range from about 60 ° C (140 ° F) to about 71 ° C (160 ° F) )

[00137] Embodiment M. The method according to claim 10, characterized in that the pressure reduction of the system of absorbent solvents with absorbed unreacted ethylene occurs at a temperature in the range of from about 71 ° C (160 ° F) to about 93 ° C (200 ° F) )

[00138] An implementation option N. The method of claim 1, further comprising:

removing at least a portion of elemental oxygen or oxygen-containing compounds from the light gas stream before contacting the light gas stream with an absorbent solvent system.

[00139] An implementation option O. A method for producing polyethylene, including:

contacting ethylene and a polymerization catalyst in a polymerization reactor under suitable reaction conditions to form a polymerization product stream;

separating the light gas stream from the polymerization product stream, said light gas stream containing unreacted ethylene;

bringing the light gas stream into contact with the absorbent solvent system in the absorption reactor at a temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), with at least a portion of the unreacted ethylene from the light gas stream being absorbed an absorbent solvent system to provide a composition comprising a complex of an absorbent solvent system and unreacted ethylene;

removal of unabsorbed gases from a stream of light gases from contact with an absorbent solvent system;

recovering unreacted ethylene from an absorbent system

solvents; and

contacting the recovered ethylene and the polymerization catalyst.

[00140] Embodiment R. The method of claim 15, further comprising:

introducing a stream containing a composition comprising a complex of an absorbent solvent system and unreacted ethylene into a solvent regenerator at a temperature in the range of from about 10 ° C (50 ° F) to about 93 ° C (200 ° F);

recovering unreacted ethylene from a composition comprising a complex of an absorbent solvent system and an unreacted ethylene to obtain recovered ethylene and a regenerated absorbent solvent system;

introducing a stream containing recovered ethylene into the polymerization reactor; and

introducing a stream containing a regenerated system of absorbent solvents into the absorption reactor.

[00141] An implementation option Q. The method according to p. 16, characterized in that the introduction of a stream containing a composition containing a complex of an absorbent solvent system and unreacted ethylene into the solvent regenerator occurs at a pressure in the range of about 0 kPa gage. (0 psig) to about 69 kPa (10 psig).

[00142] An implementation option R. The method according to p. 15, characterized in that the extraction of unreacted ethylene from the system of absorbent solvents involves lowering the pressure in the absorption reactor to a pressure in the range from about 0 kPa gage. (0 psig) to about 69 kPa (10 psig).

[00143] An implementation option S. The method of claim 15, further comprising:

removal of non-absorbed gases from the light gas stream from contact with an absorbent solvent system to form an exhaust gas stream.

[00144] Embodiment T. The method of claim 15, wherein the absorbent solvent system comprises copper chloride, aniline and N-methylpyrrolidone.

[00145] Embodiment U. The method of claim 15, wherein contacting the light gas stream with the absorbent solvent system in the absorption reactor comprises increasing the pressure in the absorption reactor to a pressure in the range of about 276 kPa gage. (40 psig) to about 414 kPa (60 psig).

[00146] An implementation option V. The method of claim 15, further comprising:

removing at least a portion of elemental oxygen or oxygen-containing compounds from the light gas stream before introducing the light gas stream into the absorption reactor.

[00147] Embodiment W. A polyethylene production system, comprising:

a feed stream containing ethylene, said feed stream being characterized in that it enters a polymerization reactor;

a stream of polymerization products, wherein said stream of polymerization products is characterized in that it leaves the polymerization reactor and enters the separator;

a stream of light gases containing unreacted ethylene, said stream of light gases being characterized by the fact that it leaves the separator, where the stream of light gases was separated from the stream of polymerization products, said stream of light gases being characterized by the fact that it enters an absorbent solvent system, said absorbent solvent system has a temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F);

an absorbent-ethylene conjugate, wherein said absorbent-ethylene conjugate is characterized in that it is formed in an absorbent solvent system by absorbing at least a portion of unreacted ethylene by an absorbent solvent system; and

an exhaust stream containing ethane, wherein said exhaust stream is characterized in that it leaves the absorption reactor, said exhaust stream comprising components of a light gas stream that have not been absorbed by an absorbent solvent system; and

a stream of recovered unreacted ethylene, wherein said stream of recovered unreacted ethylene is characterized in that it leaves the absorption reactor and again enters the polymerization reactor.

[00148] Embodiment X. The system of claim 23, wherein said recovery of the recovered unreacted ethylene from the absorbent-ethylene conjugate is due to pressure reduction from the pressure in the absorption reactor to a pressure in the range of about 0 kPa. (0 psig) to about 69 kPa (10 psig).

[00149] Embodiment Y. The system of claim 23, wherein recovering the recovered unreacted ethylene from the absorbent-ethylene conjugate occurs at a temperature in the range of about 43 ° C (110 ° F) to about 93 ° C (200 ° F). )

[00150] Embodiment Z. The system of claim 23, wherein the absorbent solvent system comprises copper chloride, aniline, and N-methylpyrrolidone.

[00151] An implementation option AA. A system for producing polyethylene, including:

a polymerization reactor, wherein said polymerization reactor is configured to produce a feed stream containing ethylene, and said polymerization reactor is configured to discharge a stream of polymerization products;

a separator, said separator being configured to receive a stream of polymerization products and to discharge a stream of light gases containing unreacted ethylene, said stream of light gases being separated from the stream of polymerization products; and

an absorption reactor comprising an absorbent solvent system, said absorption reactor configured to receive a stream of light gases, absorb at least a portion of the unreacted ethylene using an absorbent solvent system at a temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), and discharging an exhaust gas stream containing components of a light gas stream not absorbed by an absorbent solvent system, wherein the absorption reactor is further configured with the ability to release a stream of recovered unreacted ethylene, wherein said polymerization reactor is further configured to receive a stream of recovered unreacted ethylene.

[00152] An implementation option AB. The system of claim 27, wherein the recovered unreacted ethylene is recovered from the absorbent solvent system by reducing the pressure from the pressure in the absorption reactor to a pressure in the range of about 0 kPa. (0 psig) to about 69 kPa (10 psig). [00153] An embodiment of an AC. The system of claim 27, wherein the recovered unreacted ethylene is recovered from the absorbent solvent system by raising the temperature from the absorption temperature to a temperature in the range of about 43 ° C (110 ° F) to about 93 ° C (200 ° F).

[00154] An implementation option for AD. The system of claim 27, wherein said absorption reactor includes two or more reactors with a packed bed, the recovered unreacted ethylene being recovered from the absorbent solvent system by reducing pressure in one of the two or more packed bed reactors, while another reactor with a packing layer operates at a pressure in the range of about 276 kPa gage. (40 psig) to about 414 kPa (60 psig).

[00155] An implementation option AE. The system of claim 27, wherein the absorbent solvent system comprises copper chloride, aniline and N-methylpyrrolidone.

[00156] An implementation option AF. The system of claim 27, further comprising a second absorption reactor, said absorption reactors being capable of absorbing ethylene in a liquid solvent by pressure differential absorption.

[00157] an implementation Option AG. A system for producing polyethylene, including:

a polymerization reactor, wherein said polymerization reactor is configured to produce a feed stream containing ethylene, and said polymerization reactor is configured to discharge a stream of polymerization products;

a separator, said separator being configured to receive a stream of polymerization products and to discharge a stream of light gases containing unreacted ethylene, said stream of light gases being separated from the stream of polymerization products;

an absorption reactor comprising an absorbent solvent system, said absorption reactor configured to receive a stream of light gases, absorb at least a portion of the unreacted ethylene using an absorbent solvent system at a temperature in the range of from about 4 ° C (40 ° F) to about 43 ° C (110 ° F), and discharging an exhaust gas stream containing components of a light gas stream not absorbed by an absorbent solvent system, wherein the absorption reactor is further configured with the ability to produce a complex stream containing ethylene absorbed in an absorbent solvent system; and

a solvent regenerator for regenerating a system of absorbent solvents and for discharging a stream of recovered unreacted ethylene, said polymerization reactor being further configured to receive a stream of recovered unreacted ethylene.

[00158] An implementation option of AN. The system of claim 33, wherein said solvent regenerator is configured to operate at a pressure in the range of about 0 kPa gage. (0 psig) to about 69 kPa (10 psig).

[00159] An implementation option AI. The system of claim 33, wherein said solvent regenerator is configured to operate at a temperature in the range of from about 43 ° C (110 ° F) to about 93 ° C (200 ° F).

EXAMPLES

[00160] The present invention has been described generally, the following examples are given as specific embodiments of the present invention and to demonstrate the practical embodiment and advantages of the present invention. It should be understood that these examples are for illustrative purposes only and are not intended to limit the description or claims in any way.

[00161] An automated installation simulating an industrial process was used to obtain model results according to the systems and / or methods described in this application. The applicable model is shown in FIG. 9, which shows an embodiment of a system 900, as described herein, and will be used to describe examples below. In the embodiment shown in FIG. 9, the light gas stream, which was separated from the polymerization product stream of the reactor to produce polyethylene, was supplied to the absorption reactor 116. The total molar and mass flows and the molar and mass flows of the components of the light gas stream 18 are shown in Table 1 .

[00162] The unreacted ethylene entering the absorption reactor 116 was absorbed by the absorbing solvent system in the absorption reactor 116. The absorbed unreacted ethylene was introduced, as a complex stream 28, into the first regenerator 120. In the stream 28, the absorbed ethylene was heated using a REG1HEAT heat exchanger before being introduced into first regenerator 120. Ethylene was desorbed from the absorbent solvent system in the first regenerator 120 and sent as stream 29 to a second regenerator 122. Stream 29 could be cooled l using a REG2COOL heat exchanger before introducing it into the second regenerator 122. Ethylene was recovered as stream 20. The absorbent solvent in streams 32 and 34 was combined in a FEEDCOOL heat exchanger to return to absorption reactor 116 as stream 30.

[00163] Table 2 shows the operating conditions for examples 1-44 of ethylene recovery using the system 900 shown in figure 9. For the examples shown in table 2, the system of absorbent solvents contained a system of copper chloride, aniline and NMP, and the composition of the purified product calculated based on 90% ethylene recovery. The composition of the purified product recovered according to figure 9, included ethylene, ethane, nitrogen, hydrogen and isobutane. The mass% of each of these components in the purified product is shown in table 2. The compositions of the purified product shown in the table are the compositions of stream 20 in figure 9. Selected examples from table 2 are discussed in more detail below.

EXAMPLE 3

[00164] In Example 3 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of -9 ° C (15 ° F), at a temperature of the regenerated solvent of -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 kPa gage. (0psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, the system 900 recovered 90% of ethylene, the solvent circulation was 156388 kg / h (344776 l / h) and the amount of ethylene in the purified product was 64.5%.

EXAMPLE 4

[00165] In Example 4 of Table 2, the operating conditions were the same as in Example 3, except that the first regenerator 120 was operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, the system 900 recovered 90% ethylene, the solvent circulation was 65198 kg / h (143736 f / h) and the purified product contained 77.5% ethylene.

EXAMPLE 7

[00166] In Example 7 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 12 ° C (53 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 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 kPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, the system 900 extracted 90% ethylene; the solvent circulation was 24458 kg / h (53920 l / h). The composition of the purified product for example 7 is shown in table 2.

[00167] When comparing example 7 with examples 3 and 4, the flow rate of the solvent 24458 kg / h (53920 f / h) in example 7 was lower than the costs 65198 kg / h (143736 f / h) and 156388 kg / h ( 344776 f / h) in Examples 3 and 4. Example 7 showed that the solvent circulation required for ethylene absorption in an absorbent solvent system containing copper chloride, aniline and NMP was much lower for an absorption temperature of 12 ° C (53 ° F) ) than for an absorption temperature of -9 ° C (15 ° F) due to an unexpected drop in the solubility of ethylene in the system of absorbent solvents at temperatures below but 10 ° C (50 ° F).

EXAMPLE 8

[00168] In Example 8 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 13 ° C (55 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 276 kPa gage. (40 psig). The first regenerator 120 operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 kPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, system 800 recovered 90% of ethylene; the solvent circulation was 21675 kg / h (47785 f / h). The composition of the purified product for example 8 is shown in table 2.

[00169] Example 8 confirmed the results obtained in example 7 that lower solvent circulation costs are required if the absorption reactor operates at a temperature of 13 ° C (55 ° F) rather than at temperatures below 10 ° C (50 ° F). Examples 2 further showed that changing the temperature of the regenerators 120 from 66 ° C (150 ° F) to 93 ° C (200 ° F) did not significantly affect the flow rate of the solvent.

EXAMPLE 19

[00170] In Example 19 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 12 ° C (53 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 276 kPa gage. (40 psig). The first regenerator 120 operated at a temperature of 93 ° C (200 ° F) and a pressure of 69 kPa gage. (10 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 69 kPa gage. (10 psig). Under these conditions, system 900 recovered 90% of ethylene; the solvent circulation was 26885 kg / h (59272 f / h). The composition of the purified product is shown in table 2.

[00171] Example 19 confirmed the lower solvent circulation rates discussed in Examples 7 and 8, compared with Examples 3 and 4. Example 19 also showed that the pressure change in the first and second regenerators 120 and 122 from 0 kPa. (0 psig) up to 69 kPa (10 psig) slightly changed the results. The action of regenerators 120 and 122 at 0 kPa h. (0 psig) can provide lower solvent circulation as well as improved product purity, and the action of regenerators 120 and 122 at 69 kPa gage. (10 psig) may provide a safer design because positive pressure in the regenerators 120 and 122 reduces the likelihood of air leakage in the system and method, which can interact with copper chloride in the system of absorbent solvents and slow performance.

EXAMPLE 28

[00172] In Example 28 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 11 ° C (52 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 414 kPa gage. (60 psig). The first regenerator 120 operated at a temperature of 38 ° C (100 ° F) and a pressure of 0 kPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, system 900 recovered 90% of ethylene; the solvent circulation was 26586 kg / h (58613 f / h). The composition of the purified product is shown in table 2.

[00173] Under the conditions of Example 28, the solvent circulation rate was lower than in Examples 3 and 4, and the amount of ethylene in the purified product was significantly higher.

EXAMPLE 29

[00174] In Example 29 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 13 ° C (55 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 414 kPa gage. (60 psig). The first regenerator 120 operated at a temperature of 66 ° C (150 ° F) and a pressure of 0 kPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, system 900 recovered 90% of ethylene; the solvent circulation was 23181 kg / h (51106 f / h). The composition of the purified product is shown in Table 2.

[00175] Under the conditions of Example 29, the solvent circulation rate was less than in Examples 3 and 4, and the amount of ethylene in the purified product was significantly higher.

EXAMPLE 30

[00176] In Example 30 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 13 ° C (56 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 414 kPa gage. (60 psig). The first regenerator 120 operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 kPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, the system 900 extracted 90% ethylene; the solvent circulation rate was 21203 kg / h (46744 f / h). The composition of the purified product is shown in table 2.

[00177] Under the conditions of Example 30, the solvent circulation was less than in Examples 3 and 4, and the amount of ethylene in the purified product was significantly higher.

EXAMPLE 33

[00178] In Example 33 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 39 ° C (102 ° F), at a temperature of the regenerated solvent of 38 ° C (100 ° F). The absorption reactor 116 also operated at a pressure of 414 kPa gage. (60 psig). The first regenerator 120 operated at a temperature of 93 ° C (200 ° F) and a pressure of 0 kPa gage. (0 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 0 kPa gage. (0 psig). Under these conditions, the system 900 extracted 90% ethylene; the solvent circulation rate was 28774 kg / h (63,435 f / h). The composition of the purified product is shown in table 2.

[00179] Under the conditions of Example 33, the solvent circulation rate was less than in Examples 3 and 4, and the amount of ethylene in the purified product was significantly higher. In addition, example 33 showed that the action of the absorption reactor 116 at temperatures higher than the maximum solubility temperature shown in figure 7, for example, at 39 ° C (102 ° F) as shown in example 33, can still be economically feasible. since, for example, the cost of circulation of the solvent remains low compared with the conditions of examples 3 and 4.

EXAMPLE 40

[00180] In Example 40 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 11 ° C (52 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 414 kPa gage. (60 psig). The first regenerator 120 operated at a temperature of 66 ° C (150 ° F) and a pressure of 69 kPa. (10 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 69 kPa. (10 psig). Under these conditions, the system 900 extracted 90% ethylene; the solvent circulation was 26055 kg / h (57441 f / h). The composition of the purified product is shown in table 2.

[00181] Under the conditions of Example 40, the circulation rate of the solvent was less than in Examples 3 and 4, and the amount of ethylene in the purified product was significantly higher.

EXAMPLE 41

[00182] In Example 41 of Table 2, the absorption reactor 116 of Figure 9 was operated at a temperature of 13 ° C (55 ° F), at a temperature of the regenerated solvent of 10 ° C (50 ° F). The absorption reactor 116 also operated at a pressure of 414 kPa gage. (60 psig). The first regenerator 120 operated at a temperature of 93 ° C (200 ° F) and a pressure of 69 kPa gage. (10 psig). The second regenerator 122 operated at a temperature of 10 ° C (50 ° F) and a pressure of 69 kPa gage. (10 psig). Under these conditions, the system 900 recovered 90% of ethylene; the solvent circulation rate was 23352 kg / h (51482 f / h). The composition of the purified product is shown in table 2.

[00183] Under the conditions of Example 41, the solvent circulation rate was lower than in Examples 3 and 4, and the amount of ethylene in the purified product was significantly higher.

MODELING EXAMPLES

[00184] An automated installation simulating an industrial process was used to obtain model output according to the systems and / or methods described in this application. The model used is shown in FIG. 10, where a gaseous stream designated VAPFEED (for example, a stream of light gases as described herein) was supplied 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 designating the various streams in Table 3 correspond to the streams shown in Figure 10. In figure 10, ASORB1 is an absorption reactor shown as a four-stage absorber operating at 90 ° F.

[00185] At least one embodiment has been described, and variants, combinations and / or modifications of the embodiment (s) and / or features of the embodiment (s) made by one of ordinary skill in the art are within the scope of the present invention. Alternative embodiments obtained by combining, combining and / or eliminating features of an embodiment (s) are also included in the scope of the present invention. If numerical ranges or limitations are explicitly indicated, such explicit ranges or limitations should be understood as including iterative ranges or restrictions of a similar magnitude falling within explicitly indicated ranges or limitations (e.g., 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 with a lower boundary R1 and an upper boundary Ru is described, any number falling within the specified range is definitely described. In particular, the following numbers in the range are specifically described: R = R ₁ + k * (R _u -R ₁ ), where k is a variable ranging from 1 percent to 100 percent in increments of 1 percent, i.e. to 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 defined by two R numbers, as indicated above, is also specifically described. The use of the term "optionally" with respect to any element of a claim means that the element is necessary, or, alternatively, the element is not necessary, both alternatives are included in the scope of the claim. The use of broader terms, such as includes, contains and has, should be understood as providing support for narrower terms, such as consists of, consists essentially of and is formed essentially of. Accordingly, the scope of protection is not limited to the above description, but is determined by the following claims, the scope includes all equivalents of the subject matter of the claims. Any and every claim is included as additional disclosure in the description, and claims are embodiments of the described subject matter. Discussion of the links in the description is not an assumption that they represent the prior art, especially any link that has a publication date earlier than the priority date of this application. A description of all patents, patent applications, and publications referenced herein is incorporated into this application by reference, to the extent that they enrich the present application with examples, techniques, or other details.

Claims (63)

1. A method of extracting ethylene from a stream of polymerization products of a polyethylene production system, comprising: separating the light gas stream from the polymerization product stream, said light gas stream containing unreacted ethylene; bringing into contact the stream of light gases with a system of absorbent solvents, and the specified contacting stream of light gases with a system of absorbing solvents occurs at a temperature in the range from 4 ° C (40 ° F) to 43 ° C (110 ° F), and at least as part of the unreacted ethylene from the light gas stream is absorbed by an absorbent solvent system; and recovering unreacted ethylene from 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, characterized in that the contacting of the stream of light gases with a system of absorbent solvents occurs at a temperature in the range from 4 ° C (40 ° F) to 16 ° C (60 ° F). 3. The method according to claim 1, characterized in that the contacting of the stream of light gases with a system of absorbent solvents occurs at a temperature of 10 ° C (50 ° F). 4. The method according to p. 1, characterized in that the contacting of the stream of light gases with a system of absorbent solvents occurs at a temperature in the range from 16 ° C (60 ° F) to 32 ° C (90 ° F). 5. The method of claim 1, further comprising introducing into the system of absorbent solvents a stripping gas, wherein at least a portion of said stripping gas is absorbed by the system of absorbent solvents. 6. The method according to p. 5, characterized in that said stripping gas is selected from the group consisting of nitrogen and isobutane. 7. The method according to p. 1 or 5, characterized in that bringing into contact the stream of light gases with a system of absorbent solvents includes sparging the stream of light gases through a layer of packing in a system of absorbent solvents. 8. The method according to p. 1 or 5, characterized in that bringing into contact the stream of light gases with a system of absorbent solvents includes increasing the pressure of the stream of light gases and a system of absorbing solvents to a pressure in the range from 276 kPa gage. (40 psig) up to 414 kPa (60 psig). 9. The method according to p. 1 or 5, characterized in that the extraction of unreacted ethylene from the system of absorbent solvents involves lowering the pressure of the system of absorbent solvents with absorbed unreacted ethylene at a temperature in the range from 43 ° C (110 ° F) to 93 ° C (200 ° F). 10. The method according to p. 9, characterized in that the pressure reduction of the system of absorbent solvents occurs at a pressure in the range from 0 kPa gage. (0 psig) up to 69 kPa (10 psig). 11. The method according to p. 9, characterized in that the pressure reduction of the system of absorbent solvents with absorbed unreacted ethylene occurs at a temperature in the range from 60 ° C (140 ° F) to 71 ° C (160 ° F). 12. The method according to p. 9, characterized in that the pressure reduction of the system of absorbent solvents with absorbed unreacted ethylene occurs at a temperature in the range from 71 ° C (160 ° F) to 93 ° C (200 ° F). 13. The method of claim 1 or 5, further comprising removing at least a portion of the elemental oxygen or oxygen-containing compounds from the light gas stream before bringing the light gas stream into contact with the absorbent solvent system. 14. A method of producing polyethylene, including: contacting ethylene and a polymerization catalyst in a polymerization reactor under suitable reaction conditions to form a polymerization product stream; separating the light gas stream from the polymerization product stream, said light gas stream containing unreacted ethylene; bringing the light gas stream into contact with the absorbent solvent system in the absorption reactor at a temperature in the range of 4 ° C (40 ° F) to 43 ° C (110 ° F), with at least a portion of the unreacted ethylene from the light gas stream being absorbed by the absorbing system solvents to obtain a composition containing a complex system of absorbent solvents and unreacted ethylene; removal of unabsorbed gases from a stream of light gases from contact with an absorbent solvent system; recovering unreacted ethylene from an absorbent solvent system; and contacting the recovered ethylene and the polymerization catalyst, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone. 15. The method according to p. 14, further comprising: introducing a stream containing a composition comprising a complex of an absorbent solvent system and unreacted ethylene into a solvent regenerator at a temperature in the range of 10 ° C (50 ° F) to 93 ° C (200 ° F); recovering unreacted ethylene from a composition comprising a complex of an absorbent solvent system and an unreacted ethylene to obtain recovered ethylene and a regenerated absorbent solvent system; introducing a stream containing recovered ethylene into the polymerization reactor; and introducing a stream containing a regenerated system of absorbent solvents into the absorption reactor. 16. The method according to PP. 14, 15, characterized in that the introduction of the stream containing the composition containing the complex system of absorbent solvents and unreacted ethylene in the solvent regenerator occurs at a pressure in the range from 0 kPa gage. (0 psig) up to 69 kPa (10 psig). 17. The method according to p. 14, characterized in that the extraction of unreacted ethylene from the system of absorbent solvents involves lowering the pressure in the absorption reactor to a pressure in the range from 0 kPa gage. (0 psig) up to 69 kPa (10 psig). 18. The method according to PP. 14, 15 or 17, further comprising removing unabsorbed gases from the light gas stream from contact with the absorbent solvent system to form an exhaust gas stream. 19. The method according to p. 18, further comprising processing the exhaust gas stream in a processing device, said processing device comprising a cracking device, a catalytic cracking device, a scrubber, a converter, a processing device, a dehydrogenation device, an oxygen removal device, a torch, or a combination specified devices. 20. The method according to PP. 14, 17 or 19, characterized in that bringing into contact the flow of light gases with a system of absorbent solvents in the absorption reactor includes increasing the pressure in the absorption reactor to a pressure in the range from 276 kPa gage. (40 psig) up to 414 kPa (60 psig). 21. The method according to PP. 14, 17 or 19, further comprising removing at least a portion of elemental oxygen or oxygen-containing compounds from the light gas stream before introducing the light gas stream into the absorption reactor. 22. A system for producing polyethylene, including: a feed stream containing ethylene, said feed stream being characterized in that it enters a polymerization reactor; a stream of polymerization products, wherein said stream of polymerization products is characterized in that it leaves the polymerization reactor and enters the separator; a stream of light gases containing unreacted ethylene, said stream of light gases being characterized by the fact that it leaves the separator, where the stream of light gases was separated from the stream of polymerization products, said stream of light gases being characterized by the fact that it enters an absorbent solvent system, said absorbent solvent system has a temperature in the range of 4 ° C (40 ° F) to 43 ° C (110 ° F); an absorbent-ethylene conjugate, wherein said absorbent-ethylene conjugate is characterized in that it is formed in an absorbent solvent system by absorbing at least a portion of unreacted ethylene by an absorbent solvent system; and an exhaust stream containing ethane, wherein said exhaust stream is characterized in that it leaves the absorption reactor, said exhaust stream comprising components of a light gas stream that have not been absorbed by an absorbent solvent system; and a stream of recovered unreacted ethylene, wherein said stream of recovered unreacted ethylene is characterized in that it leaves the absorption reactor and again enters the polymerization reactor, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone. 23. The system according to p. 22, characterized in that said extraction of the recovered unreacted ethylene from the absorbent and ethylene conjugate occurs by reducing the pressure from the pressure in the absorption reactor to a pressure in the range from 0 kPa gage. (0 psig) up to 69 kPa (10 psig). 24. The system according to p. 24 or 25, characterized in that the extraction of the extracted unreacted ethylene from the conjugate of the absorbent and ethylene occurs at a temperature in the range from 43 ° C (110 ° F) to 93 ° C (200 ° F). 25. A system for producing polyethylene, including: a polymerization reactor, wherein said polymerization reactor is configured to produce a feed stream containing ethylene, and said polymerization reactor is configured to discharge a stream of polymerization products; a separator, said separator being configured to receive a stream of polymerization products and to discharge a stream of light gases containing unreacted ethylene, said stream of light gases being separated from the stream of polymerization products; and an absorption reactor containing a system of absorbent solvents, wherein said absorption reactor is configured to receive a stream of light gases, absorb at least a portion of unreacted ethylene using a system of absorbent solvents at a temperature in the range of 4 ° C (40 ° F) to 43 ° C ( 110 ° F), and discharging an exhaust gas stream comprising components of a light gas stream not absorbed by an absorbent solvent system, the absorption reactor being further configured to discharge accelerate the flow of recovered unreacted ethylene, wherein said polymerization reactor is further configured to receive a stream of recovered unreacted ethylene, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone. 26. The system according to p. 25, characterized in that the recovered unreacted ethylene is recovered from the system of absorbent solvents by reducing the pressure from the pressure in the absorption reactor to a pressure in the range from 0 kPa gage. (0 psig) up to 69 kPa (10 psig). 27. The system according to p. 25 or 26, characterized in that the recovered unreacted ethylene is recovered from the system of absorbent solvents by raising the temperature from the absorption temperature to a temperature in the range from 43 ° C (110 ° F) to 93 ° C (200 ° F) . 28. The system according to p. 25 or 26, characterized in that said absorption reactor includes two or more reactors with a packing layer, the recovered unreacted ethylene being recovered from the absorbing solvent system by reducing the pressure in one of said two or more reactors with a packing layer, while another reactor with a packing layer operates at a pressure in the range of 276 kPa gage. (40 psig) up to 414 kPa (60 psig). 29. The system of claim 25 or 26, further comprising a second absorption reactor, said absorption reactors being capable of absorbing ethylene in a liquid solvent using pressure differential absorption. 30. A system for producing polyethylene, including: a polymerization reactor, wherein said polymerization reactor is configured to produce a feed stream containing ethylene, and said polymerization reactor is configured to discharge a stream of polymerization products; a separator, said separator being configured to receive a stream of polymerization products and to discharge a stream of light gases containing unreacted ethylene, said stream of light gases being separated from the stream of polymerization products; an absorption reactor containing a system of absorbent solvents, wherein said absorption reactor is configured to receive a stream of light gases, absorb at least a portion of unreacted ethylene using a system of absorbent solvents at a temperature in the range of 4 ° C (40 ° F) to 43 ° C ( 110 ° F), and discharging an exhaust gas stream comprising components of a light gas stream not absorbed by an absorbent solvent system, the absorption reactor being further configured to discharge accelerate a complex stream containing ethylene absorbed in an absorbent solvent system; and a solvent regenerator for regenerating a system of absorbent solvents and for discharging a stream of recovered unreacted ethylene, wherein said polymerization reactor is further configured to receive a stream of recovered unreacted ethylene, moreover, the system of absorbent solvents contains copper chloride, aniline and N-methylpyrrolidone. 31. The system of claim 30, wherein said solvent regenerator is configured to operate at a pressure in the range of 0 kPa. (0 psig) up to 69 kPa (10 psig). 32. The system according to p. 30 or 31, characterized in that said solvent regenerator is configured to operate at a temperature in the range of 43 ° C (110 ° F) to 93 ° C (200 ° F). 33. The system of claim 30 or 31, further comprising a processing device configured to receive an exhaust gas stream. 34. The system of claim 33, wherein said processing device includes a cracking device, a catalytic cracking device, a scrubber, a converter, a processing device, a dehydrogenation device, an oxygen removal device, a torch, or a combination of these devices.

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