CN104245088A

CN104245088A - Component separations in polymerization

Info

Publication number: CN104245088A
Application number: CN201380019547.XA
Authority: CN
Inventors: S·E·库费尔德; J·D·浩托威; 章艾茀
Original assignee: Chevron Phillips Chemical Co LLC
Current assignee: Chevron Phillips Chemical Co LLC
Priority date: 2012-04-13
Filing date: 2013-04-04
Publication date: 2014-12-24
Anticipated expiration: 2033-04-04
Also published as: MX2014012363A; IN2014DN08508A; CA2869960A1; WO2013154907A2; WO2013154907A3; SG11201406524VA; RU2619690C2; EP2836284A2; RU2014140971A; CN104245088B

Abstract

A process for component separation in a polymer production system, comprising separating a polymerization product stream into a gas stream and a polymer stream, wherein the gas stream comprises ethane and unreacted ethylene, distilling the gas stream into a light hydrocarbon stream, wherein the light hydrocarbon stream comprises ethane and unreacted ethylene, contacting the light hydrocarbon stream with an absorption solvent system, wherein at least a portion of the unreacted ethylene from the light hydrocarbon stream is absorbed by the absorption solvent system, and recovering a waste gas stream from the absorption solvent system, wherein the waste gas stream comprises ethane, hydrogen, or combinations thereof.

Description

Component seperation in polymerization

The cross reference of related application

The application submitted on October 15th, 2010, exercise question is the U.S. Patent Application Serial 12/905 of " ethylene separation (Improved Ethylene Separation) of improvement ", the part of 966 continues, its by reference with its entirety in order to all objects are incorporated to herein.

Background

Technical field

The disclosure relates generally to poly production.More specifically, the disclosure relates to the system and method improving polyethylene production efficiency by reducing ethylene loss.

Background technology

Produce polymer such as polyethylene by lighter-than-air gas and require highly purified monomer and comonomer raw material.Due to boiling point difference little between lighter-than-air gas in this raw material, industrial production high-purity raw can require the operation of multiple destilling tower, high pressure and low temperature.So, relevant to purification of raw materials cost of energy accounts for the remarkable ratio of producing this base polymer totle drilling cost.In addition, the foundation structure produce, kept and recycle high-purity raw to require is the signal portion of relevant capital cost.

In order to make up some costs and make production maximize, regaining and/or recycle any unreacted unstrpped gas, especially light hydrocarbon reactant, such as ethene, can be useful.The gas comprising unreacted monomer can be separated with polymer after polymerization.Process polymer, reclaims unreacted monomer from the gas regained after polymerization simultaneously.In order to realize this point, the air-flow of withdrawal is conventionally sent through purification process or is redirected by other unnecessary treatment steps.In each case, reclaim the conventional method of monomer and need disadvantageous on energy and the process of costliness.

Thus, need efficiently being separated of ethene and recirculation flow.

Summary of the invention

Disclosed herein is the method for Component seperation in polymer production system, comprise and polymerizate stream is separated into air-flow and polymer flow, wherein air-flow comprises ethane and unreacted ethene; Airflow distillation is become lightweight hydrocarbon stream, wherein lightweight hydrocarbon stream comprises ethane and unreacted ethene; Make lightweight hydrocarbon stream and lyosoption system contacts, wherein from the unreacted at least partially ethene of lightweight hydrocarbon stream by lyosoption Systemic absorption; With from lyosoption system recoveries waste gas streams, wherein waste gas streams comprise ethane, hydrogen or its combination.

Also disclose the method for Component seperation in polymer production system herein, comprise and polymerizate stream is separated into air-flow and polymer flow, wherein air-flow comprises ethane and unreacted ethene; Hydrocarbon stream and the first bottom stream in the middle of airflow distillation is become, wherein, hydrocarbon stream comprises ethane, ethene and isobutene; Middle hydrocarbon stream is distilled into lightweight hydrocarbon stream and the second bottom stream, wherein lightweight hydrocarbon stream comprises ethane and ethene; Make lightweight hydrocarbon stream and lyosoption system contacts, wherein from the unreacted at least partially ethene of lightweight hydrocarbon stream by lyosoption Systemic absorption; With from lyosoption system recoveries waste gas streams, wherein waste gas streams comprise ethane, hydrogen or its combination.

There is further disclosed herein the method for Component seperation in polymer production system, comprise and olefinic monomer is polymerized in the first polymer reactor, with m-polymerizate stream in producing; By in m-polymerizate stream be separated in m-air-flow and in m-polymer flow, wherein, m-air-flow comprises ethane, unreacted ethene and hydrogen; With make in m-polymer flow be polymerized in the second polymer reactor.

There is further disclosed herein the method for Component seperation in polymer production system, comprise and olefinic monomer is polymerized in the first polymer reactor; By in m-polymerizate stream be separated in m-air-flow and in m-polymer flow, wherein, m-air-flow comprises ethane and unreacted ethene; M-polymer flow is polymerized in the second polymer reactor; Scavenger is introduced with before the second polymer reactor.

There is further disclosed herein the method for Component seperation in polymer production system, comprise and olefinic monomer is polymerized in the first polymer reactor, with m-polymerizate stream in producing; Make from the hydrogen at least partially of m-polymerizate stream degassed, to produce the product stream that hydrogen reduces; By hydrogen reduce product stream be separated in m-air-flow and in m-polymer flow, wherein, m-air-flow comprises ethane and unreacted ethene; With make in m-polymer flow be polymerized in the second polymer reactor.

The aforementioned characteristic sum technical advantage rather broadly outlining open subject matter, can understand following detailed description better.When those skilled in the art read preferred embodiment following detailed description and referring to accompanying drawing time, above-mentioned various feature, and other features are apparent.

Accompanying drawing explanation

In order to describe the preferred embodiment of open method and system in detail, description, wherein:

The schematic diagram of the first embodiment of Fig. 1 diagram polyethylene production system;

The schematic diagram of the second embodiment of Fig. 2 diagram polyethylene production system;

The schematic diagram of the third embodiment of Fig. 3 diagram polyethylene production system;

The schematic diagram of the 4th kind of embodiment of Fig. 4 diagram polyethylene production system;

The schematic diagram of the 5th kind of embodiment of Fig. 5 diagram polyethylene production system;

The flow chart of the first embodiment of Fig. 6 diagram polyethylene process;

The flow chart of the second embodiment of Fig. 7 diagram polyethylene process;

The flow chart of the third embodiment of Fig. 8 diagram polyethylene process;

The flow chart of the 4th kind of embodiment of Fig. 9 diagram polyethylene process;

Figure 10 diagram has the schematic diagram of the embodiment of the absorption reactor thermally of pressure swing absorption structure;

Figure 11 is that the solubility of ethene and ethane in diagram lyosoption system is to the figure of temperature;

The schematic diagram of the embodiment of the absorption system of Figure 12 diagram simulation; With

The schematic diagram of the embodiment of the absorption system of Figure 13 diagram simulation.

Detailed description of the invention

System, the apparatus and method relevant to having the polyethylene production of improving efficiency are disclosed herein.This system, apparatus and method relate generally to be separated the first chemical constituent or compound from composition, and described source is from poly production and comprise the first chemical constituent or compound and one or more other chemical constituents, compound or analogs.

With reference to figure 1, disclose the first polyethylene production (PEP) system 100.PEP system 100 generally comprises clarifier 102, reactor 104,106, separator 108, processor 110, destilling tower 122, absorption reactor thermally 116 and treatment facility 114.In PEP embodiment disclosed herein, various system component can through being suitable for transporting concrete stream---such as by Fig. 1-5,10, the stream of numbering in 12-13 shows in detail---one or more conduits (such as, pipe, pipe-line system, flowline etc.) fluid be communicated with.

In the embodiment of figure 1, incoming flow 10 can be communicated to clarifier 102.The incoming flow 11 of purification can be communicated to one or more reactor 104,106 from clarifier 102.Wherein this system comprises two or more reactors, and reactor stream 15 can be communicated to reactor 106 from reactor 104.Hydrogen can be introduced into reactor 106 to flow 21.Polymerizate stream 12 can be communicated to separator 108 from one or more reactor 104,106.Polymer flow 14 can be communicated to processor 110 from separator 108.Product stream 16 can send from processor 110.Air-flow 18 can be communicated to destilling tower 122 from separator 108.Distillation bottom stream 23 can send from destilling tower 122, and effluent 27 can send from destilling tower 122.Lightweight hydrocarbon stream 25 can send from destilling tower 122 and be communicated to absorption reactor thermally 116.Waste gas streams 20 can be communicated to treatment facility 114 from absorption reactor thermally 116, and recirculation flow 22 can be communicated to other positions system 100 from absorption reactor thermally 116, such as, be communicated to clarifier 102 through separator 108.When being recycled to clarifier 102 through separator 108, recirculation flow 22 can be communicated to separator 108 from absorption reactor thermally 116, and stream can be communicated to clarifier 102 from separator 108.

With reference to figure 2, disclose the second PEP system 200, it has many system components common with PEP100.In the Alternate embodiments of Fig. 2 explaination, the second PEP system 200 comprises degasifier 118 in addition.Replace the first PEP system 100 (as explained in Fig. 1), in the embodiment of Fig. 2 explaination, air-flow 18 can be communicated to degasifier 118.The air-flow 26 of process can be communicated to destilling tower 122 from degasifier 118.Consider that the embodiment of present subject matter can operate when being with or without degasifier 118 of the gas component that can be suitable in air-flow 18.

In the optional embodiment of Fig. 2 explaination, the second PEP system 200 comprises destilling tower 124 in addition.In the embodiment comprising destilling tower 122 and 124, destilling tower 122 can be described as the first destilling tower or redistillation tower, and destilling tower 124 can be described as after-fractionating tower or light destilling tower.As shown in Figure 2, the air-flow of process 26 (with optionally, there is no the air-flow 18 of the embodiment of degasifier 118) destilling tower 122 can be communicated to.Middle hydrocarbon stream 29 can be communicated to destilling tower 124 from destilling tower 122.Distillation bottom stream 23 can send from destilling tower 122.Distillation bottom stream 33, and optionally, effluent 31 can send from destilling tower 124.Lightweight hydrocarbon stream 25 can be issued to absorption reactor thermally 116 from destilling tower 124.

With reference to figure 3, disclose the third PEP system 300, it has many system components common with PEP system 100 and 200.The system component in polymerizate stream 12 downstream, show in such as Fig. 1 and 2 those, not included in Fig. 3; But, consider that the embodiment of such as system 300 can be included in this downstream components in various open embodiment.In the optional embodiment of Fig. 3 explaination, the third PEP system 300 comprises the separator 105 between reactor 104 and reactor 106 alternatively.Scavenger can be introduced into system through flowing 35.Stream 35 can with in m-polymerizate stream 15 be communicated to separator 105, wherein m-polymerizate stream 15 in being separable into m-air-flow 19 and in m-polymer flow 17.In m-polymer flow 17 can be communicated to reactor 106, it sends polymerizate stream 12.In m-air-flow 19 can be communicated to absorption reactor thermally 116, it sends waste stream 20, absorbent stream 30 and recirculation flow 22.Waste stream 20 can be communicated to treatment facility 114 from absorption reactor thermally 116, and recirculation flow 22 can be communicated to other positions system 300 from absorption reactor thermally 116, as in Fig. 1 to described by recirculation flow 22.

With reference to figure 4, disclose the 4th kind of PEP system 400, it has many system components common with PEP system 300.The system component in polymerizate stream 12 downstream, show in such as Fig. 1 and 2 those, not included in Fig. 4; But, consider that the embodiment of such as system 400 can be included in this downstream components in various open embodiment.In the optional embodiment of explaining in the diagram, the 4th kind of PEP system 400 comprises separator 126 alternatively.Reactor 104 is m-polymerizate stream 15 in can sending, and it can be communicated to separator 126.Hydrogen stream 37 can send from separator 126 product stream 39 reduced with hydrogen can be communicated to separator 105 from separator 126.

With reference to figure 5, disclose the 5th kind of PEP system 500, it has many system components common with PEP system 300 and 400.The system component in polymerizate stream 12 downstream, show in such as Fig. 1 and 2 those, not included in Fig. 5; But, consider that the embodiment of such as system 500 can be included in this downstream components in various open embodiment.In the optional embodiment of Fig. 5 explaination, the 5th kind of PEP system 500 comprises regenerator 120 (such as, desorption container) in addition.Substitute PEP system 100,200,300 and 400, in the embodiment of explaining in Figure 5, combined-flow 28 can be communicated to regenerator 120 from absorption reactor thermally 116.Recirculation flow 22 can be communicated to other positions in system 500, such as, is communicated to clarifier 102 (as discussed in figure 1) through separator.The absorbent stream 30 of regeneration can be communicated to absorption reactor thermally 116 from regenerator 120.Although regenerator 120 shows in Figure 5 in conjunction with absorption reactor thermally 116, consider that regenerator can be used for any absorption reactor thermally 116 of the embodiment of composition graphs 1 to 4 in addition.In addition, consider that the absorption reactor thermally 116 of Fig. 5 can be configured to not operate when there is no regenerator 120.

The temperature of lean solvent can take from the stream 30 in Fig. 5.The temperature of absorption reactor thermally 116 can be depending on the heat of the temperature of lean solvent in the temperature of air-flow 18, stream 30, the heat of solution and reaction.In disclosed embodiment, large 50 to 300 times of the mass velocity of the comparable air-flow of mass velocity 18 of lean solvent in stream 30.So the temperature of absorption reactor thermally 116 highly can depend on the temperature of the lean solvent in disclosed embodiment.

Disclose the various embodiments of suitable PEP system, disclose now the embodiment of PEP method.Can with reference to one or more embodiments of one or more description PEP methods of PEP system 100, PEP system 200, PEP system 300, PEP system 400 and/or PEP system 500.Although given PEP method can be described with reference to one or more embodiments of PEP system, thisly openly should not be construed as so restrictive.Although the various steps of method disclosed herein can disclose or explaination with concrete order, should not be construed as and the carrying out of these methods is restricted to any order specifically, unless otherwise noted.

With reference to figure 6, explain the first PEP method 600.PEP method 600 generally comprises at block 61 purified feed stream, the monomer polymerization of purified feed stream is made at block 62, to form polymerizate, at block 63, polymerizate is separated into polymer flow and air-flow, polymer flow is processed at block 64, at block 65 from flow separation at least one gas component, to form recirculation flow and waste stream, with at block 66 combustion waste stream.

As an example, the first PEP method 600 or its part can through the first PEP system 100 (such as, as explained in Fig. 1) enforcements.With reference to figure 1 and 6, in embodiments, incoming flow 10 can comprise gas reactant, especially ethene.In embodiments, purified feed stream can produce purification stream 11, and it comprises substantially pure monomer (such as, vinyl monomer), comonomer (such as, butene-1 comonomer) or its combination.Make the monomer of purification stream 11 (optionally, comonomer) polymerization can produce polymerizate stream 12, it generally comprises unreacted monomer (such as, ethene), optional unreacted comonomer (such as, butene-1), accessory substance (such as, ethane, it can be the accessory substance ethane formed by ethene and hydrogen) and polymerizate (such as, polymer and optionally, copolymer).Separation of polymeric product stream 12 can produce polymer flow 14 (such as, polyethylene polymer, copolymer) and air-flow 18, it generally comprises unreacted monomer (such as, vinyl monomer and any optional comonomer such as butene-1) and various gas (such as, ethane, hydrogen).Process polymer flow 14 can produce product stream 16.Recirculation flow 22 can be produced from air-flow 18 separating at least one gas component---it generally comprises unreacted vinyl monomer (optionally, unreacted comonomer), and waste gas streams 20.In embodiments, the ethene of distillation from air-flow 18 can be comprised, to produce lightweight hydrocarbon stream 25 from air-flow 18 separating at least one gas component.In embodiments, alternatively or additionally, separation bubble 18 can comprise the ethene absorbed from air-flow 18, to produce waste gas streams 20 and then to discharge the ethene of absorption, to form recirculation flow 22.Recirculation flow 22, comprises ethene, can pressurized (such as, returning clarifier 102 for pressurization through separator 108) and to reboot into PEP method (such as, PEP method 600).Burner exhaust stream 20 can apply a torch (flare) carry out as treatment facility 114.

With reference to figure 7, explaination the second PEP method 700, it has many method steps common with PEP method 600.PEP method 700 generally comprises at block 71 purified feed stream, the monomer polymerization of purified feed stream is made at block 72, with m-polymerizate in formation, in polymerizate is separated into by block 73 m-polymer flow and in m-air-flow, monomer (optionally, the comonomer) polymerization of m-polymer flow in block 74 makes, in block 75 therefrom m-flow separation at least one gas component, to form recirculation flow and waste stream, with at block 76 combustion waste stream.In the optional embodiment of Fig. 7 explaination, the block 63-64 of Fig. 6 is replaced by block 73-75.Generally speaking, the method 700 of Fig. 7 occurs between reactor 104 and 106, and the method 600 of Fig. 6 occurs in the downstream of reactor 104 and 106.

As an example, the second PEP method 700 or its part can through the third PEP system 300 (such as, as illustrated in fig. 3) enforcements.With reference to figure 3 and 7, in embodiments, incoming flow 10 can comprise gas reactant, especially ethene.In embodiments, purified feed stream can produce purification stream 11, and it comprises substantially pure monomer (such as, vinyl monomer) and optionally, comonomer (such as, butene-1).M-polymerizate stream 15 during the monomer polymerization of purification stream 11 can be produced, it generally comprises unreacted monomer (such as, ethene), optional unreacted comonomer (such as, butene-1), accessory substance (such as, ethane, it can be the accessory substance ethane formed by ethene and hydrogen) and polymerizate (such as, polymer and optionally, copolymer).At the polymerizate stream 12 of Fig. 1---it is in downstream of polymer reactor 104 and 106---substitute in, in Fig. 3, in embodiment, m-polymerizate stream 15 can between polymer reactor (one or more) 104 and polymer reactor (one or more) 106.In separation, in can producing, m-polymer flow 17---it generally comprises unreacted ethene, ethane (it can be the accessory substance ethane formed by ethene and hydrogen) and polymer (such as m-polymerizate stream 15, polyethylene), with in m-air-flow 19, it generally comprises unreacted monomer (such as, vinyl monomer), optionally unreacted comonomer is (such as, butene-1 monomer) and various gas (such as, ethane, hydrogen).In making, monomer (optionally, the comonomer) polymerization of m-polymer flow 17 can produce polymerizate stream 12.The component of polymerizate stream 12 can according to the embodiment process of system in Fig. 1 and 2 100 and 200.Therefrom m-air-flow 19 separating at least one gas component can produce recirculation flow 22---and it generally comprises unreacted vinyl monomer (optionally, comonomer), and waste gas streams 20.In embodiments, therefrom m-air-flow 19 separating at least one gas component can comprise therefrom m-air-flow 19 and absorbs ethene, to produce waste gas streams 20 and then to discharge the ethene of absorption, to form recirculation flow 22.Recirculation flow 22, comprises ethene, can be pressurized and reboot and (such as, as depicted in figure 1) enter PEP method (such as, PEP method 700).Burner exhaust stream 20 can apply a torch and to carry out as treatment facility 114.

With reference to figure 8, explain the third PEP method 800, it has many method steps common with PEP method 600 (that is, block 61,62,63,64,65 and 66).In the optional embodiment of Fig. 8 explaination, PEP method 800 comprises block 81 flow of process air, with the air-flow of formation processing with in the flow separation at least one gas component of block 65 ' from process, to form recirculation flow and waste stream.

In embodiments, the third PEP method 800 or its part can through the second PEP system 200 (such as explaining in Fig. 2) enforcements.The embodiment of alternate figures 1 and 6, in the embodiment of Fig. 2 and 8, flow of process air 18 can produce the air-flow 26 of process.In embodiments, flow of process air 18 comprises and makes air-flow 18 deoxidation.Recirculation flow 22 can be produced from the air-flow 26 separating at least one gas component of process---it generally comprises unreacted vinyl monomer (optionally, comonomer), waste gas streams 20, distillation bottom stream 23, distillation bottom stream 33 and effluent 31.

With reference to figure 9, explain the 4th kind of PEP method 900, it has many method steps common with PEP method 700.In the optional embodiment of Fig. 9 explaination, PEP method 900 comprises block 91 flow of process air (such as, m-air-flow 19) with the air-flow of formation processing.The block 75 of Fig. 7 changes at block 75 ', for the flow separation at least one gas component from process, to form combined-flow and waste gas streams.Comprise in block 92, PEP method 900 and combined-flow is separated into absorbent stream and recirculation flow.

In embodiments, the 4th kind of PEP method 900 or its part can through the 5th kind of PEP system 500 (such as explaining in Fig. 5) enforcements.Replace the embodiment of Fig. 3 and 7, in the embodiment of Fig. 5 and 9, unreacted monomer-absorbent (such as, ethene-absorbent) can be produced from the air-flow 41 separating at least one gas component of process combined-flow 28.In embodiments, the ethene that unreacted monomer-absorbent combined-flow 28 comprises release absorption is separated, to form recirculation flow 22 and absorbent stream 30.In the embodiment of Fig. 5 and 9, unreacted comonomer-absorbent (such as, butene-1-absorbent) can be produced from the air-flow 26 separating at least one gas component of process combined-flow 28.In embodiments, be separated unreacted comonomer-absorbent in combined-flow 28 and comprise the comonomer of release absorption, to form the absorbent stream 30 of recirculation flow 22 and regeneration.

In one or more embodiments disclosed herein, purified feed stream (such as, at block 61 or 71) can comprise and is separated undesired compound and element from the incoming flow comprising ethene, to form purified feed stream.In embodiments, incoming flow can comprise ethene and other gases various, is such as but not limited to methane, ethane, acetylene, propylene, has other hydrocarbon various of three or more carbon atoms, or its combination.In embodiments, purified feed stream can comprise any suitable method or technique, comprise non-limitative example filtration, membrane choosing, with various chemicals react, absorption and sorption, distillation (one or more) or its combine.

In the embodiment that such as Fig. 1-5 explains, purified feed stream can comprise transmission incoming flow 10 to clarifier 102.In one or more embodiments disclosed herein, clarifier 102 can comprise equipment or the device of one or more reactant gas in the incoming flow being suitable for purifying and comprising multiple potential undesired gaseous compound, element, pollutant or analog.The non-limitative example of suitable clarifier 102 can comprise filter, film, reactor, absorbent, molecular sieve, one or more destilling tower or its combination.Clarifier 102 can be configured to from comprising separating ethene following stream: methane, ethane, acetylene, propane, propylene, water, oxygen other gaseous hydrocarbons various, various pollutant and/or its combination.

In embodiments, purified feed stream can produce the purified feed 11 comprising substantially pure ethene.In embodiments, purified feed stream can comprise and be less than 25% by the total weight of this stream, alternatively, is less than about 10%, alternatively, is less than the nitrogen of about 1.0%, oxygen, methane, ethane, propane or its any one or multiple combined." substantially pure ethene " as used herein refer to fluid stream comprise by this stream total weight at least about 60% ethene, alternatively, at least about the ethene of 70%, alternatively, at least about the ethene of 80%, alternatively, at least about 90% ethene, alternatively, at least about the ethene of 95%, alternatively, at least about 99% ethene, alternatively, by this stream total weight at least about 99.5% ethene.In embodiments, incoming flow 11 can comprise the ethane of trace further, such as, by come into question from recirculation flow.

In one or more embodiments disclosed herein, can make incoming flow 11, in m-polymerizate stream 15 and in monomer polymerization in m-polymer flow 17.In one or more embodiments, the monomer polymerization of purified feed (such as, at block 62 and 72) can be comprised and make be suitable for contacting polymerisation between multiple monomer under the condition forming polymer with antigravity system by a kind of monomer or various of monomer.In one or more embodiments disclosed herein, make the comonomer of purified feed be polymerized (such as, at block 62 and 72) can comprise and make be suitable for contacting polymerisation between multiple comonomer under the condition forming copolymer with antigravity system by a kind of comonomer or multiple comonomer.Similarly, in one or more embodiments disclosed herein, in making, the monomer polymerization (such as, at block 74) of m-polymer flow can comprise and makes be suitable for contacting polymerisation between multiple monomer under the condition forming polymer with antigravity system by a kind of monomer or various of monomer.In one or more embodiments disclosed herein, in making, comonomer polymerization (such as, at block 74) of m-polymer flow can comprise and makes be suitable for contacting polymerisation between multiple comonomer under the condition forming copolymer with antigravity system by a kind of comonomer or multiple comonomer.Still similarly, in one or more embodiments disclosed herein, in making, the monomer polymerization of m-polymerizate can comprise and makes be suitable for contacting polymerisation between multiple monomer under the condition forming polymer with antigravity system by a kind of monomer or various of monomer.In one or more embodiments disclosed herein, in making, the comonomer polymerization of m-polymerizate can comprise and makes be suitable for contacting polymerisation between multiple comonomer under the condition forming copolymer with antigravity system by a kind of comonomer or multiple comonomer.

As Fig. 1-5 in the embodiment of explaining, the monomer polymerization of purified feed can be comprised and sends incoming flow 11 to one or more polymer reactor or " reactor " 104,106.In the embodiment of such as Fig. 1-2 explaination, in making, the monomer polymerization of m-polymerizate can comprise m-polymerizate stream 15 to polymer reactor (one or more) 106 in transmission.In the embodiment of such as Fig. 1-2 explaination, in making, the monomer polymerization of m-polymerizate can comprise and sends m-polymerizate stream 15 to polymer reactor (one or more) 106 in auto polymerization reactor (one or more) 104.In the embodiment that such as Fig. 3-5 explains, in making, the monomer polymerization of m-polymer flow 17 can comprise m-polymer flow 17 to polymer reactor (one or more) 106 in transmission.In the embodiment that such as Fig. 3-5 explains, in making, the monomer polymerization of m-polymer flow 17 can comprise and sends m-polymer flow 17 to polymer reactor (one or more) 106 in self-separation device 105.

In embodiments, any suitable antigravity system can be adopted.Suitable antigravity system can comprise catalyst and, optionally, co-catalyst and/or promoter.The non-limitative example of suitable antigravity system comprises ziegler natta catalyst, Ziegler catalyst, chrome catalysts, chromium oxide catalyst, two chromium catalysts, metallocene catalyst, Raney nickel or its combination.Be suitable for the antigravity system of disclosure use at such as U.S. Patent number 7,619,047 and U.S. Patent Application Publication No. 2007/0197374,2009/0004417,2010/0029872,2006/0094590 and 2010/0041842 in describe, its each section is incorporated to herein with its entirety by reference.

In one or more embodiments disclosed herein, reactor 104,106 combinations that can comprise following any container or container, it is suitable for being configured to being provided in the presence of a catalyst, and monomer is (such as, ethene) and/or polymer is (such as, " activity " or growing polymer chain), optionally comonomer (such as, butene-1) and/or copolymer between chemical reaction to produce polymer (such as, polyethylene polymer) and/or the environment (such as, contact zone) of copolymer.Although the embodiment of explaination illustrates the various PEP systems with two tandem reactors in Fig. 1,2 and 3, but read of the present disclosure those skilled in the art will recognize that and can adopt a reactor, alternatively, the reactor of any suitable quantity and/or structure.

As used herein, term " polymer reactor " or " reactor " comprise can polymerization of olefin monomers or comonomer to produce any polymer reactor of homopolymers or copolymer.This homopolymers and copolymer are called resin or polymer.Various types of reactor comprises those that can be described as batch reactor, slurry-phase reactor, Gas-phase reactor, solution reactor, high-pressure reactor, tubular reactor or autoclave reactor.Gas-phase reactor can comprise fluidized-bed reactor or classification horizontal reactor.Slurry-phase reactor can comprise vertical or horizontal loop.High-pressure reactor can comprise autoclave or tubular reactor.Type of reactor can comprise method in batches or continuously.Continuation method can use interval or continuous product discharge.Method also can comprise partially or completely directly recycling of unreacted monomer, unreacted comonomer and/or diluent.

Polymerization reactor system of the present disclosure can comprise the reactor of the type in system or multiple reactors of identical or different type.In multiple reactor, the production of polymer can comprise the several stages at least two separation of polymeric reactors, described at least two separation of polymeric reactors are by transfer stream (one or more), pipeline (one or more), device (one or more) (such as, separation container (one or more)) and/or equipment (one or more) is (such as, valve or other mechanisms) be interconnected, making may by by the first polymer reactor (such as, reactor 104) in produce polymer be transferred to the second reactor (such as, reactor 106).The polymerizing condition of the expectation in a reactor may be different from the operating condition of other reactors.Alternatively, the polymerization in multiple reactor can comprise from a reactor manual transfer polymer to reactor subsequently, for continuing polymerization.Multiple reactor assembly can comprise any combination, and it includes but not limited to the combination of the combination of multiple loop reactor, multiple gas reactor, loop and gas reactor, multiple high-pressure reactor or high pressure and loop and/or gas reactor.Multiple reactor can serial or parallel connection operation.

In the embodiment of explaination in such as Fig. 1-5, produce polymer in multiple reactor and can comprise at least two polymer reactors 104,106, it is interconnected by one or more equipment or device (such as, valve, continuously delivery valve (take-off valve) and/or continuous output machine structure).In the embodiment of explaining in such as Fig. 1-2, produce polymer and can comprise at least two polymer reactors 104,106 in multiple reactor, it is interconnected by one or more stream or pipeline (such as, m-polymerizate stream 15).As in Fig. 3-5 in the embodiment of explaining, produce polymer in multiple reactor and can comprise at least two polymer reactors 104,106, it by one or more separator (such as, separator 105 and/or separator 126) be interconnected through two or more streams (such as, m-polymerizate stream 15 and in m-polymer flow 17).

According to an aspect, polymerization reactor system can comprise the loop slurry-phase reactor that at least one comprises vertical or horizontal loop.Monomer, diluent, catalyst and optionally any comonomer can continuous feed to the loop reactor wherein occurring to be polymerized.Generally speaking, continuation method can comprise and monomer, optional comonomer, catalyst and diluent introduced polymer reactor continuously and is continuously removed the suspension comprising polymer beads and diluent from this reactor.Reactor effluent can be flashed, to shift out solid polymer from the liquid comprising diluent, monomer and/or comonomer.Various technology can be used for this separating step, includes but not limited to flash distillation, and it can comprise any combination of heating and decompression; By the separation of whirlwind effect in cyclone separator or cyclone hydraulic separators; Or by centrifugal separation.

In one or more embodiments, comonomer can comprise the unsaturated hydrocarbons with 3 to 12 carbon atoms.Such as, comonomer can comprise propylene, butene-1, hexene-1, octene or its combination.

Such as, at U.S. Patent number 3,248,179,4,501,885,5,565,175,5,575,979,6,239,235,6,262,191 and 6,833, disclose typical slurry phase polymerisation process (also referred to as method for forming particles) in 415, its each section is incorporated to herein with its entirety by reference.

In one or more embodiments, the suitable diluent used in slurry polymerization includes but not limited to by the monomer be polymerized, and optionally comonomer, and is the hydrocarbon of liquid at reaction conditions.The example of suitable monomer diluent includes but not limited to hydrocarbon such as propane, cyclohexane, iso-butane, normal butane, pentane, isopentane, neopentane and n-hexane.In embodiments, comonomer diluent can comprise the unsaturated hydrocarbons with 3 to 12 carbon atoms.The example of suitable comonomer diluent includes, but are not limited to propylene, butene-1, hexene-1, octene or its combination.Carry out under the reaction of some Loop Polymerizations can not use the bulk conditions of diluent wherein.An example is the polymerization of propylene monomer, as U.S. Patent number 5, and 455, disclosed in 314, it is incorporated to herein with its entirety by reference.

According to still on the other hand, polymer reactor can comprise at least one Gas-phase reactor.This type systematic can adopt continuous recirculation flow, and it comprises one or more monomers being continuously circulated through fluid bed under polymerization conditions in the presence of a catalyst.Recirculation flow can be fetched from fluid bed and recycle and get back to reactor.Meanwhile, polymer product can be fetched from reactor and new or fresh monomer can be added, to replace the monomer of polymerization.Similarly, optionally fetch copolymer products from reactor and new or fresh comonomer can be added, to replace the comonomer of polymerization, the monomer of polymerization or its combination.This Gas-phase reactor can comprise the method for alkene multistep gas-phase polymerization, and wherein alkene is polymerized at least two independently gas-phase polymerization district with gas phase, polymer to the second polymeric area comprising catalyst that charging is simultaneously formed in the first polymeric area.U.S. Patent number 5,352,749,4588,790 and 5,436, disclose the Gas-phase reactor of a type in 304, its each section is incorporated to herein with its entirety by reference.

According to still on the other hand, reactors for high pressure polymerisation can comprise tubular reactor or autoclave reactor.Tubular reactor can have several district, wherein can add fresh monomer (optionally, comonomer), initator or catalyst.Monomer (optionally, comonomer) can be entrained in inert gas and in a district of reactor and introduce.Initator, catalyst and/or catalytic component can be carried secretly in the gas flow and introduce in another district of reactor.Air-flow can be mixed for polymerization.Can suitably adopt heat and pressure to obtain optimum polymerizating reacting condition.

According to still on the other hand, polymer reactor can comprise solution polymerization reactor, and wherein monomer (optionally, comonomer) contacts with carbon monoxide-olefin polymeric by suitable stirring or other means.The carrier comprising inertia organic diluent or excess monomer (optionally, comonomer) can be adopted.If expected, when presence or absence fluent material, monomer and/or optional comonomer can contact with catalytic reaction products in the gas phase.Under polymeric area remains on the temperature and pressure making to form polymer solution in reaction medium.Can adopt to stir and control to obtain better temperature and maintain homogeneous polymerization mixture throughout polymeric area.Suitable means are used for dissipation polymerization exotherm.

The polymer reactor being suitable for system and method for the present disclosure can comprise following any combination further: at least one feed system of at least one raw material feed system, catalyst or catalytic component and/or at least one polymer recovery system.Suitable reactor assembly can comprise further for following system: purification of raw materials, catalyst store and prepare, extrude, reactor cooling, polymer recovery, fractionation, recirculation, storage, discharging, lab analysis and process control.

Control be used for polymerization efficiency and provide the condition of resin properties to comprise the concentration of temperature, pressure and various reactant.Polymerization temperature can affect catalyst production, polymer molecular weight and molecular weight distribution.Suitable polymerization temperature can be any temperature lower than the temperature that depolymerizes according to Gibbs Free energy equation.Usually this comprises from about 60 DEG C to about 280 DEG C, and such as, and from about 70 DEG C to about 110 DEG C, this depends on the type of polymer reactor.

Suitable pressure also will change according to reactor and polymeric type.Usually 1000psig is less than for the pressure of liquid phase polymerization in loop reactor.For the pressure of gas-phase polymerization usually at about 200 – 500psig.High pressure polymerisation in tubulose or autoclave reactor, generally about 20, carries out under 000 to 75,000psig.Operate in the critical zone that polymer reactor also can occur under general higher temperature and pressure.On the critical point of Pressure/Temperature figure, the operation of (supercritical phase) can provide advantage.In embodiments, polymerization can occur in the environment with suitable temperature and pressure combination.Such as, polymerization can in scope from about 550psi to about 650psi, alternatively, under the pressure of about 600psi to about 625psi and scope from about 170 ℉ to about 230 ℉, alternatively, carry out to the temperature of about 220 ℉ from about 195 ℉.

The concentration of various reactant can be controlled to produce the resin with some Physical and mechanical properties of polyoropylene.The resin properties being determined expectation by resin and the whole purposes product of the method formation forming this product of recommending.Engineering properties comprises stretching, bending, impact, creep, stress relaxation and hardness test.Physical property comprises density, molecular weight, molecular weight distribution, melting temperature, glass transition temperature, the melting temperature (temperature melt of crystallization) of crystallization, density, stereospecicity, crackle increase, long chain branching and rheology measurement value.

The concentration of monomer, comonomer, hydrogen, co-catalyst, modifier and electron donor and/or dividing potential drop are important for these resin properties of production.Comonomer can be used for controlling product density.Hydrogen can be used for controlling molecular weight of product.Co-catalyst can be used for alkylation, removes poisonous substance and control molecular weight.Modifier can be used for controlling product characteristics and influenced By Electron Donors stereospecicity, molecular weight distribution or molecular weight.In addition, because poisonous substance impact reaction and product characteristics, the concentration of poisonous substance is minimized.

In embodiments, polymerization single polymerization monomer can comprise and suitable antigravity system introduced the first and/or second reactor 104,106 respectively, to form slurry.Alternatively, suitable antigravity system can residue in the first and/or second reactor 104 respectively, in 106.

As explained above, polymerization single polymerization monomer can comprise the one or more polymeric reaction condition of selective manipulation, with produce given polymer product, with produce there is one or more desirable properties polymer product, with the efficiency realizing expecting, to realize the productive rate etc. expected or its combination.The non-limitative example of this parameter comprises the type of temperature, pressure, catalyst or co-catalyst and/or the concentration of amount and various reactant and/or dividing potential drop.In embodiments, the monomer polymerization of purified feed 52 is made can to comprise the one or more polymeric reaction condition of adjustment.In embodiments, polymerization single polymerization monomer can comprise vinyl monomer and/or comonomer such as butylene are added into polymer reactor 106.

In embodiments, polymerization single polymerization monomer keeps suitable temperature, pressure and/or dividing potential drop (one or more) during can being included in polymerisation, circulate alternatively during polymerisation between a series of suitable temperature, pressure and/or dividing potential drop (one or more).

In embodiments, polymerization single polymerization monomer can comprise hydrogen is introduced one or more reactor 104 and 106.Such as, Fig. 1 and 2 explains hydrogen and is introduced into reactor 106 by flowing 21.Adjustable introduces the amount of the hydrogen of reactor 106 so that the mol ratio obtaining hydrogen and ethene in diluent is 0.001 to 0.1.This mol ratio can be at least 0.004 in reactor 106.In embodiments, this mol ratio can be no more than 0.05.In the diluent of reactor 104, the concentration of hydrogen can be at least 20 with the ratio of the hydrogen concentration of polymer reactor 106, alternatively, and at least 30, alternatively, at least 40, alternatively, be not more than 300, alternatively, be not more than 200.At U.S. Patent number 6,225, disclose suitable hydrogen concentration control method and system in 421, it is incorporated to herein by reference.

In embodiments, polymerization single polymerization monomer can comprise monomer (optionally, comonomer), antigravity system and/or slurry at reactor 104, in 106 and/or between circulation, flowing, running, mixing, stir or its combination.Monomer (optionally wherein, comonomer), in the embodiment that is recycled of antigravity system and/or slurry, the speed of circulation (such as, slurry rate) can be from about 1m/s to about 30m/s, alternatively, from about 2m/s to about 17m/s, alternatively, from about 3m/s to about 15m/s.

In embodiments, polymerization single polymerization monomer can comprise configuration reactor 104,106, to produce multi-modal (such as, bimodal) polymer (such as, polyethylene).Such as, resulting polymers can comprise relative HMW, low-density (HMWLD) polyethylene polymer and low relative molecular amount, high density (LMWHD) polyethylene polymer.Such as, various types of suitable polymer can be characterized by and have various density.Such as, I type can be characterized by and have scope from about 0.910g/cm ³to about 0.925g/cm ³density, alternatively, II type can be characterized by be had from about 0.926g/cm ³to about 0.940g/cm ³density, alternatively, type III can be characterized by be had from about 0.941g/cm ³to about 0.959g/cm ³density, alternatively, IV type can be characterized by have and be greater than about 0.960g/cm ³density.

In embodiments, polymerization single polymerization monomer can comprise makes comonomer at one or more polymer reactor 104, is polymerized in 106.

In the embodiment of explaining in figs. 1-5, m-polymerizate stream 15 and/or polymerizate stream 12 during the monomer polymerization of purified feed can be produced.In this, m-polymerizate stream 15 and/or polymerizate stream 12 can generally comprise various solid, semisolid, volatility and non-volatile liquid, gas and its combination.In embodiments, in, m-polymerizate stream 15 and/or polymerizate stream 12 can comprise hydrogen, nitrogen, methane, ethene, ethane, propylene, propane, butane, iso-butane, pentane, hexane, hexene-1 and heavy hydrocarbon.In embodiments, the scope that ethene exists can from about 0.1% to about 15% by the total weight of stream, alternatively, and from about 1.5% to about 5%, alternatively, about 2% to about 4%.The scope that ethane exists can from about 0.001% to about 4% by the total weight of stream, alternatively, and from about 0.2% to about 0.5%.The scope that iso-butane exists can from about 80% to about 98% by the total weight of stream, alternatively, and from about 92% to about 96%, alternatively, about 95%.

Solid and/or liquid can comprise polymer product (such as, polyethylene polymer), are commonly referred to " polymer fluff (fluff) " in this stage of PEP method.Gas can comprise unreacted, gas reactant monomer or optional comonomer (such as, unreacted vinyl monomer, unreacted butene-1 monomer), off-gas product, gaseous contaminant or its combination.

In one or more embodiments disclosed herein, polymerizate is separated into polymer flow and air-flow (such as, at block 63) can generally comprise and shift out any gas by any suitable method from liquid and/or solid (such as, polymer fluff).

In the embodiment of such as Fig. 1-2 explaination, polymerizate is separated into polymer flow and air-flow and can comprises and send polymerizate stream 12 to separator 108.

In embodiments, air-flow 18 can comprise hydrogen, nitrogen, methane, ethene, ethane, propylene, propane, butane, iso-butane, pentane, hexane, hexene-1 and heavy hydrocarbon.In embodiments, the scope that ethene exists can from about 0.1% to about 15% by the total weight of stream, alternatively, and from about 1.5% to about 5%, alternatively, about 2% to about 4%.The scope that ethane exists can from about 0.001% to about 4% by the total weight of stream, alternatively, and from about 0.2% to about 0.5%.The scope that iso-butane exists can from about 80% to about 98% by the total weight of stream, alternatively, and from about 92% to about 96%, alternatively, about 95%.

In one or more embodiments, by in m-polymerizate be separated in m-polymer and in m-air-flow (such as, at block 73) can generally comprise and shift out any gas by any suitable method from liquid and/or solid (such as, polymer fluff).

As in Fig. 3 and 5 in the embodiment of explaining, by m-polymerizate be separated in m-polymer flow with in m-air-flow can be separated in the single step comprising m-polymerizate stream 15 to separator 105 in transmission in complete.

In embodiment as illustrated in fig. 3, by m-polymerizate be separated in m-polymer flow and in m-air-flow can comprise therefrom m-polymerizate stream 15 separating at least one gas component.Therefrom m-polymerizate stream 15 separating at least one gas component in can producing m-air-flow 19 and in m-polymer flow 17.In m-polymerizate stream 15 can comprise hydrogen, ethene, ethane, polymer, iso-butane or its combination.In m-air-flow 19 can comprise hydrogen, ethene, ethane or its combination.In m-polymer flow 17 can comprise polymer, iso-butane or its combination.

In embodiment as illustrated in fig. 3, by m-polymerizate be separated in m-polymer flow and in m-air-flow can comprise m-polymerizate in reduction pressure so as flash distillation ethene, hydrogen, ethane or its combination.In m-polymerizate stream 15 can comprise hydrogen, ethene, ethane, polymer, iso-butane or its combination.Separator 105 can produce pressure reduce, thus ethene, hydrogen and ethane therefrom m-polymerizate is separated or flash distillation so that generation comprise m-air-flow 19 in hydrogen, ethene and ethane.

As in Fig. 5 in the embodiment of explaining, by m-polymerizate be separated in m-polymer flow and in m-air-flow can be included in reactor 106 before introduce scavenger.In embodiments, scavenger can reduce the concentration of component such as hydrogen.The embodiment display stream 35 of Fig. 3 and 5 explaination can before reactor 106 in such as m-polymerizate stream 15 introduce.Alternatively, flow 35 can introduce separator 105 or in m-polymer flow 17.Stream 35 can comprise scavenger.In embodiments, scavenger can comprise catalyst.In embodiments, catalyst can comprise hydrogenation catalyst.Undesirably be limited by theory, scavenger can be used for consuming hydrogen, to form ethane, can reduce hydrogen concentration even to zero-dose.In embodiments, hydrogenation catalyst can have low activity for poly polymerization.Hydrogenation catalyst can comprise the metallocene catalyst of following general formula:

Cp ₂MX _n

Wherein Cp is the cyclopentadienyl group replaced; M is the transition metal of the periodic table of elements IVB race from vanadium; X is halogen or the alkyl with 1 to 10 carbon atom; And the chemical valence that n is metal M subtracts 2.In embodiments, metallocene catalyst can comprise Cp ₂tiCl ₂, also referred to as cyclopentadienyl titanium dichloride.The amount that can introduce of metallocene catalyst by m-polymerizate stream 15 weighing scale of inert diluent can be 2 to 50ppm, alternatively, 2 to 20ppm.

As in Fig. 5 in the embodiment of explaining, polymer production ability can be improved by the concentration of hydrogen in scavenger reduction stream before the second polymer reactor 106, such as, compared with in polymer reactor 104, relatively more heavy polymer can be produced in polymer reactor 106.Such as, wherein in expected response device 106 relatively more heavy polymer embodiment in, usually do not add extra hydrogen to reactor 106, because the hydrogen concentration increased in reactor 106 is harmful to producing more heavy polymer usually.Do not introduce hydrogen in this embodiment, hydrogenation catalyst can be introduced in reactor 106 or before reactor 106 and introduce.The embodiment display hydrogenation catalyst of Fig. 3 and 5 explaination can to flow 35 introducings before reactor 106.In one or more embodiments, the polymer of generation can comprise polyethylene.In this embodiment, Ziegler-Natta catalyst can be used as polymerization catalyst, and can comprise metallocene catalyst by the hydrogenation catalyst that stream 35 is introduced.The amount of the metallocene catalyst used can be make metallocene catalyst and Ziegler-Natta catalyst mass ratio (namely, g metallocene/g Z-N) scope can from about 0.1 to about 2.0, preferably from about 0.25 to about 1.5, more preferably about 0.5-1.0.In embodiments, metallocene catalyst can comprise the metallocene of non-bridging.In embodiments, the metallocene of non-bridging can comprise molybdenyl dichloride (cyclopentadienyl group) titanium, also referred to as cyclopentadienyl titanium dichloride.U.S. Patent number 6,730,751,6,221,982 and 6,291, disclose suitable hydrogenation catalyst in 601, it is by reference to being incorporated to herein.

As in Fig. 5 in the embodiment of explaining, by m-polymerizate be separated in m-polymer flow and in m-air-flow can comprise therefrom m-polymerizate stream separating at least one gas component further.In this embodiment, enter m-polymerizate stream 15 in separator 105 and can comprise unreacted hydrogen, unconverted ethene, ethane, polymer, iso-butane or its combination.In m-air-flow 19 can comprise hydrogen, ethene, ethane or its combination; And in m-polymer flow 17 can comprise polymer, iso-butane or its combination.In in m-air-flow 19 amount of ethane can be greater than the amount of unreacted hydrogen and/or unconverted ethene.

As in Fig. 4 in the embodiment of explaining, by in m-polymerizate be separated in m-polymer flow and in m-air-flow (such as, at block 73) can comprise m-polymerizate stream 15 to separator 126 in transmission and send self-separation device 126 hydrogen reduce product stream 39 to separator 105 two steps be separated in realize.

As in Fig. 4 in the embodiment of explaining, by m-polymerizate be separated in m-polymer flow and in m-air-flow can comprise make from the hydrogen at least partially of m-polymerizate degassed.Embodiment display separator 126 as Fig. 4 explaination can produce stream 37 and 39.Stream 37 can comprise the hydrogen shifted out, and flows the product that 39 can comprise hydrogen minimizing.Separator 126 can make from the hydrogen at least partially of m-polymerizate stream 15 degassed through reducing pressure.Decompression can be less than or equal to polymerization temperature in reactor 104, alternatively, is greater than 20 DEG C, alternatively, occurs at the temperature of at least 40 DEG C.Decompression can occur under the pressure being less than pressure in reactor 104.Decompression can be less than 1.5MPa.Decompression can be at least 0.1MPa.The amount of hydrogen residual in the stream 39 that in Fig. 4, hydrogen reduces can be less than 1% by the weighing scale of the amount of the hydrogen existed initial in the mixture reclaimed from reactor 104, alternatively, is less than 0.5% by weight, alternatively, and 0wt% by weight.U.S. Patent number 6,225,412 disclose suitable degassing conditions and device, and it is incorporated to herein by reference.

As in Fig. 4 in the embodiment of explaining, by m-polymerizate be separated in m-polymer flow and in m-air-flow can comprise the product stream separating at least one gas component reduced from hydrogen further.In this embodiment, the product stream 39 that the hydrogen entering separator 105 reduces can comprise hydrogen, ethene, ethane, polymer, iso-butane or its combination.In m-air-flow 19 can comprise hydrogen, ethene, ethane or its combination; And in m-polymer flow 17 can comprise polymer, iso-butane or its combination.The amount of the hydrogen existed in m-air-flow 19 in Fig. 4 can be less than 1% by the weighing scale of the amount of the hydrogen existed initial in the mixture reclaimed from reactor 104, alternatively, is less than 0.5% by weight, alternatively, and 0wt% by weight.

In one or more embodiments disclosed herein, separator 105,108 and 126 can be configured to by stream (such as, comprise poly in m-polymerizate, comprise poly polymerizate, comprise poly hydrogen reduce product) be separated into gas, liquid, solid or its combination.Product stream 12,15 and 39 can comprise unreacted, gaseous monomer or optional comonomer (such as, unreacted vinyl monomer, unreacted butene-1 monomer), off-gas product and/or gaseous contaminant.As in Fig. 4 in the embodiment of explaining, in m-polymerizate stream 15 can comprise hydrogen.In the embodiment of explaining in such as Fig. 1-2, polymerizate stream 12 can comprise hydrogen.As used herein, " unreacted monomer ", such as, ethene, is introduced into the monomer that polymer reactor is not still incorporated to polymer during referring to polymerisation.As used herein, " unreacted comonomer ", such as, butene-1, introduces the comonomer that polymer reactor is not still incorporated to polymer during referring to polymerisation.

In embodiments, separator 105,108 and/or 126 can comprise gas-liquid separator.The suitable example of this separator can comprise destilling tower, flash tank, filter, film, reactor, absorbent, adsorbent, molecular sieve or its combination.In embodiments, separator comprises flash tank.Undesirably be limited by theory, this flash tank can comprise and is configured to from high temperature and/or high-pressure fluid evaporation and/or removes the container of low vapor pressure component.Separator 105,108 and/or 126 configurablely makes to enter stream and is separable into liquid stream (such as, condensate flow) and gas (such as, steam) stream.Liquid or condensate flow can comprise product (such as, polyethylene, is commonly referred to " polymer fluff ").Gas or vapor stream can comprise volatile solvent, gaseous state, unreacted monomer and/or optional comonomer, waste gas (second order reaction product, such as pollutant etc.), or its combination.Separator 105,108 and 126 configurablely makes incoming flow pass through heating, decompression or the two flash distillation, and the enthalpy flowed is increased.This can heater via, flash line heater, known other operations various or its combination realize usually in this area.Such as, two-tube flash line heater is comprised by hot water or steam heat-exchanging.The temperature that this flash line heater can increase stream reduces its pressure simultaneously.

In one or more embodiments, polymerizate is separated into polymer flow and air-flow or by m-polymerizate be separated in m-polymer flow and in m-air-flow can comprise make polymerizate distillation, evaporation, flash distillation, filtration, membrane choosing, absorption and sorption or its combine.In the embodiment of Fig. 1-2 explaination, polymerizate is separated into polymer flow gentle miscarriage anger stream 18 and polymer flow 14.In the embodiment that Fig. 3-5 explains, by m-polymerizate be separated in m-polymer flow and in m-air-flow produce in m-air-flow 19 and in m-polymer flow 17.

In one or more embodiments disclosed herein, process polymer flow (such as, at block 64) comprise any suitable method or serial of methods, it is configured to produce and can be suitable for business or industrial application, storage, transport, further process or its polymer product combined.

In the embodiment of such as Fig. 1-2 explaination, process polymer flow can comprise transmission polymer flow 14 to processor 110.Processor 110 is configurable for performing suitable process means, and its non-limitative example comprises cooling, injection moulding, fusing, granulation, blowing, extrusion molding, rotational molding, thermoforming, cast molding, similar means or its combination.Various additive and modifier can be added into polymer, to provide better process during manufacture and for the desirable properties of end-product.The non-limitative example of this additive can comprise surface modifier such as slip agent, anti-caking agent, tackifier; Antioxidant is elementary and secondary antioxidants such as; Pigment; Processing aid is paraffin/oil and fluoroelastomer such as; With specialist additive such as fire retardant, antistatic additive, scavenger, absorbent, odor enhancers and degradation agent.

In embodiments, processor 110 can be configured to and forms suitable polymer product.The non-limitative example that can be derived from the suitable polymer product of this process comprises film, powder, bead, resin, liquid or any other suitable form that those skilled in the art will recognize that.This output suitably can be used for such as one or more different consumer products or industrial product.Such as, polymer product can utilize any one or multiple different goods, includes but not limited to bottle, drum, toy, household receptacle, utensil, film product, drum, fuel tank, pipe, geomembrane (geomembrane) and lining.In a particular embodiment, processor is configured to form bead, for being transported to consumer product manufacturers.Such as, in the embodiment of Fig. 1-2 explaination, process polymer flow produces polymer product 16 (such as, the polyethylene of granulating).

In one or more embodiments disclosed herein, flow of process air (such as, at block 81) and process in m-air-flow (such as, at block 91) can comprise for removing oxygen, oxygen containing (oxygenated) compound, any suitable method of the compound of oxidation or its combination (being commonly referred to as " oxygen ") or reaction herein from air-flow.Read and of the present disclosurely those skilled in the art will recognize that suitable method or reaction.Non-limitative example for the proper method removing oxygen comprises various catalytic reaction, contacts with the known chemical species reacted with oxygen, filters, absorption and sorption, heating, cooling or its combine.

In the embodiment of such as Fig. 2 explaination, flow of process air can comprise transmission air-flow 18 to degasifier 118.In the embodiment of such as Fig. 5 explaination, in process, m-air-flow can comprise m-air-flow 19 to degasifier 118 in transmission.

In one or more embodiments disclosed herein, degasifier 118 can comprise the equipment or the device that are configured to remove oxygen from air-flow.The non-limitative example of suitable degasifier comprises various reactor (such as, fluidized-bed reactor or fixed bed), filter or its combination.Suitable degasifier 118 can be configured to minimizing, prevent or get rid of the compound that can have and make lyosoption intoxication and/or element (such as, oxygen) avoids arriving absorption reactor thermally (such as, as herein by disclosed).

In the embodiment of Fig. 2 explaination, flow of process air produces the air-flow 26 being substantially free of the process of oxygen.In the embodiment of Fig. 5 explaination, in process, m-air-flow produces the air-flow 41 being substantially free of the process of oxygen." being substantially free of oxygen " as used herein refers to that fluid stream comprises and is not more than oxygen at least about 5% by the total weight of stream, alternatively, is not more than the oxygen of about 1%, alternatively, is not more than the oxygen of about 0.1%, alternatively, be not more than the oxygen of about 0.01%.

In one or more embodiments disclosed herein, the any suitable method from Selective Separation at least the first chemical constituent the stream comprising the first chemical constituent or compound and one or more other chemical constituent, compounds etc. or compound is generally comprised from the air-flow of air-flow and/or the process separating at least one gas component (such as, at block 65,65 ', 75 or 75 ') that---is referred to as air-flow---.In various embodiments, one or more hydrocarbon can be comprised from the gas component of flow separation.The non-limitative example of this hydrocarbon comprises alkane (such as, ethane, butane, iso-butane, hexane or its combination) and alkene or olefinic monomer are (such as, ethene, hexane or its combination) or optional comonomer (such as, butene-1).In embodiments, unreacted hydrocarbon monomer can be comprised from the gas component of flow separation, such as ethene.Optionally, unreacted hydrocarbon comonomer can be comprised from the gas component of flow separation, such as propylene.In embodiments, unreacted hydrocarbon monomer can be comprised (such as from the gas component of flow separation, ethene, separately or combine with other hydrocarbon, such as, ethane, iso-butane, hexane or its combination), or optionally hydrocarbon comonomer (such as, propylene, separately or combine with other hydrocarbon, such as, iso-butane, hexane or its combination).In embodiments, ethene can be comprised from the gas component of flow separation, separately or combine with iso-butane.In embodiments, catch iso-butane can make to save the cost of the iso-butane of catching and reduce the amount of the iso-butane in flare discharge.The non-limitative example of suitable separation means comprise distillation, evaporation, flash distillation, filtration, membrane choosing, absorption and sorption, MW exclusion, size exclusion, based on the separation of polarity or its combination.

In embodiments, can comprise from flow separation at least one gas component and distill air-flow in one step (such as, the air-flow 18 of Fig. 1, the air-flow 26 of the process of Fig. 2), to make at least one gas component be separated with other gas components according to the temperature (one or more) of boiling.In this embodiment, from flow separation at least one gas component can comprise by airflow distillation become comprise ethene, ethane, optionally hydrogen or its combination lightweight hydrocarbon stream.In this embodiment, from flow separation at least one gas component can be included in distillation bottom stream collect hexane, hexene, optionally iso-butane or its combination.In other and/or optional embodiment, can comprise from flow separation at least one gas component and collect iso-butane from the effluent of destilling tower.

In the embodiment of the system 100 shown in FIG, destilling tower 122 may be configured to separated at least one gas component.Air-flow 18 can be communicated to destilling tower 122, and air-flow 18 can comprise the non-solid component (such as, nitrogen, methane, ethene, ethane, propylene, propane, butane, iso-butane, pentane, hexane, hexene-1, heavy hydrocarbon or its combination) of the polymerizate stream 12 for vapor phase.Air-flow 18 optionally comprises hydrogen, and it can be removed or be removed by the hydrogenation catalyst in polymer reactor (one or more) in the separator such as between two polymer reactors.At least one gas component can send from destilling tower 122 with lightweight hydrocarbon stream 25, and other gas components can send from destilling tower 122 to distill bottom stream 23.Fig. 1 from destilling tower 122 with at least one gas component that lightweight hydrocarbon stream 25 sends can comprise ethene and can comprise further other lighter-than-air gas (such as, ethene, ethane, methane, carbon dioxide, nitrogen, hydrogen or its combination).Such as, the amount that there is ethene in lightweight hydrocarbon stream 25 can from about 50% to about 99% by the total weight of lightweight hydrocarbon stream 25, and alternatively from about 60% to about 98%, alternatively, from about 70% to about 95%.Propylene, propane, butane, iso-butane, pentane, hexane, hexene-1, heavy hydrocarbon or its combination can be comprised with other gas components of distilling bottom stream 23 and sending from destilling tower 122.In embodiments, distillation bottom stream 23 can be free of alkene, alternatively, is substantially free of alkene, alternatively, fundamentally not containing alkene.Such as, the amount of the alkene existed in distillation bottom stream 23 can be less than about 1.0% by the total weight of distillation bottom stream 23, alternatively, is less than about 0.5%, alternatively, is less than about 0.1%.In embodiments, the effluent 27 comprising iso-butane can send from destilling tower 122 with effluent 27.

In the embodiment of explaining in such as Fig. 1, effluent 27 or distill bottom stream 23 at least partially and can be recycled.Recirculation effluent 27 or at least partially distillation bottom stream 23 can comprise, such as, through suitable pump or compressor, send effluent 27 or at least partially distill bottom stream 23 return PEP system 100 and/or by effluent 27 or at least partially distill bottom stream 23 introduce PEP system 100, such as, for reusing in the polymerization.In embodiments, effluent 27 or distill bottom stream 23 at least partially can in conjunction with various other components (catalyst, co-catalyst etc.), to form the catalyst slurry that can be introduced into one or more reactors 104,106.Do not intend being limited by theory, because effluent 27 or at least partially distill bottom stream 23 can comprise not containing alkene isobutane stream (alternatively, be substantially free of alkene, as above disclosed), effluent 27 or at least partially distill bottom stream 23 can with catalyst component (such as, catalyst, co-catalyst etc.) mix and there is no the risk of unexpected polymerisation (such as, at the pre-polymerization introducing one or more reactor).So, effluent 27 or at least partially distill bottom stream 23 can be used as not originating, for polymerisation containing the iso-butane of alkene.Make effluent 27 or distill bottom stream 23 (comprising not containing the iso-butane of alkene) recirculation at least partially can provide effective and/or cost effectively supplies the means that iso-butane operates for polymerisation process.In alternative embodiments, effluent 27 can be sent or distill bottom stream 23 at least partially to store for using in the polymerization subsequently or adopting in the method that any other is suitable.

In embodiments, at least partially effluent 27 or at least partially distill bottom stream 23 can return destilling tower 122.Such as, can effluent 27 be sent through reboiler or distill bottom stream 23 to destilling tower 122 at least partially, for other process.

Destilling tower 122 can be configured to and/or size is set to provide the separation of the gas (such as, the lightweight hydrocarbon stream 25 of Fig. 1) of proper volume.Such as, destilling tower 122 can in scope from about 50 DEG C to about 20 DEG C, alternatively, from about 40 DEG C to about 10 DEG C, alternatively, the temperature of from about 30 to about 5 DEG C, with in scope from about 14.7psia to about 529.7psia, alternatively, from about 15.7psia to about 348psia, alternatively, operate to the pressure of about 290psia from about 85psia.Destilling tower 122 can be configured to and/or be designed and sized to the separation of the air-flow (such as, the stream 26 of Fig. 2) of the air-flow 18 or process providing proper volume.As the skilled person will recognize, air-flow 18 (optionally, the air-flow of process) can retain and/or remain in any reasonable time amount in destilling tower 122, as required in enough air-flow 18 (optionally, the air-flow of process) Component seperation can be provided.In embodiments, destilling tower 122 can be equipped with at least two outlets.

In embodiments, destilling tower 122 is configurable and/or operate, make each part, number or subset comprising the expectation of the component of air-flow 18 (optionally, the air-flow of process) of the lightweight hydrocarbon stream 25 of Fig. 1, optional effluent 27 and distillation bottom stream 23.Such as, as those skilled in the art will recognize that under help of the present disclosure, the position of concrete inflow entrance or outlet, the operating parameter of destilling tower 122, air-flow 18 are (optionally, process air-flow) composition, or its combination can be made given stream can comprise concrete one or more components of air-flow 18 (optionally, the air-flow of process) by manipulation.

In alternative embodiments, can comprise from flow separation at least one gas component and distill air-flow in two steps (such as, the air-flow 26 of air-flow 18 or process), so that at least one gas component is separated according to boiling temperature (one or more) with other gas components in making to be separated first, with in case in making to be separated second at least another gas component be separated according to boiling temperature (is each or multiple) with other gas components.In this embodiment, can comprise make airflow distillation first in being separated from flow separation at least one gas component, to form middle hydrocarbon stream, it comprises ethene, ethane, hydrogen, iso-butane or its combination.In this embodiment, can be included in the distillation bottom stream of the destilling tower of the first separation from flow separation at least one gas component and collect hexane, optionally hexene or its combination.In addition, can comprise from flow separation at least one gas component in being separated second makes ethene, ethane, optionally hydrogen or its combination distill from middle hydrocarbon stream; Hexane, optionally hexene, optionally iso-butane or its combination is collected in the second distillation bottom stream be separated; Optionally collect iso-butane from the effluent of the second destilling tower be separated.

Fig. 2 display system 200 embodiment in, destilling tower 126 and 124 can be configured to from process air-flow 26 or air-flow 18 separating at least one gas component.The air-flow 26 of process and air-flow 18 can comprise with the non-solid component of the polymerizate stream 12 of vapor phase (such as, nitrogen, methane, ethene, ethane, propylene, propane, butane, iso-butane, pentane, hexane, hexene-1, heavy hydrocarbon or its combination).Air-flow 26 and the air-flow 18 of process optionally comprise hydrogen, and it can be removed or be removed by the dehydrogenation of polymer reactor (one or more) in the separator such as between two polymer reactors.Air-flow 26 or the air-flow 18 of process can be distilled, to form middle hydrocarbon stream 29.Non-distillation component in destilling tower 126 can send from destilling tower 126 to distill bottom stream 43.Effluent 45 optionally sends from destilling tower 126.

Middle hydrocarbon stream 29 can be characterized by and comprise following, alternatively, consists essentially of following, alternatively, is substantially made up of following, alternatively, be made up of: C following ₄lighter hydrocarbon (such as, butane, iso-butane, propane, ethane or methane) and any lighter-than-air gas (such as, hydrogen or nitrogen).Such as, C ₄the amount that lighter hydrocarbon and gas exist in middle hydrocarbon stream 29 can from about 80% to about 100% by the total weight of middle hydrocarbon stream, and alternatively from about 90% to about 99.999999%, alternatively from about 99% to about 99.9999%, alternatively, C ₅the amount existed in middle hydrocarbon stream 29 with heavy hydrocarbon can from 0% to about 20% by the total weight of middle hydrocarbon stream, and alternatively from about 10% to about 0.000001%, alternatively from about 1.0% to about 0.0001%.Also such as, by the air-flow 26 of process or the weighing scale at least 90% of air-flow 18, alternatively, at least 98%, alternatively, the C of at least 99% ₄lighter hydrocarbon and gas can be present in middle hydrocarbon stream 29.

In embodiments, distillation bottom stream 43 can be characterized by and comprise C ₆heavier ratio of component as alkane, that is, is greater than the alkane (such as, heptane and/or other large alkane) of hexane.In embodiments, C ₆hydrocarbon more outside heavy paraffin hydrocarbon to be less than about 15%, alternatively, can be less than about 10% by the total weight of distillation bottom stream 43, and alternatively, the amount being less than about 5% is present in distillation bottom stream 43.In embodiments, distillation bottom stream 43 can be directed to other treatment step or method, or they can be appropriately processed alternatively.In embodiments, distill bottom stream 43 and can be directed to torch for the treatment of falling.

In embodiments, effluent 45 can be characterized by and comprise hexene.Such as, hexene can be present in effluent 45 from the amount of about 20% to about 98%, alternatively from about 40% hexene to about 95% hexene, alternatively from about 50% hexene to about 95% hexene by the total weight of effluent 45.

In embodiments, effluent 45 can be recycled.In the embodiment of Fig. 2, effluent 45 is recycled can be comprised, and such as, through suitable pump or compressor, sends effluent 45 and returns PEP system 200 and/or effluent 45 is introduced PEP system 200, such as, for reusing in the polymerization.Effluent 45 (such as, comprising hexene) is recycled can provide effective and/or cost effectively supplies the means that hexene operates for polymerisation process.In embodiments, the hexene of effluent 45 can be used as in the polymerization, such as, and the comonomer in reaction.In alternative embodiments, effluent 45 can be sent to store, for using in the polymerization subsequently or adopting in the method that any other is suitable.

In embodiments, destilling tower 126 can be equipped with one or more entrance and at least two outlets.Destilling tower 126 suitable, such as, can operate under can being suitable for the temperature and pressure of the Component seperation realizing the air-flow 26 or air-flow 18 processed.Such as, destilling tower 126 can in scope from about 15 DEG C to about 233 DEG C, alternatively, from about 20 DEG C to about 200 DEG C, alternatively, from the temperature of about 20 DEG C to about 180 DEG C, and/or in scope from about 14.7psi to about 527.9psi, alternatively, from about 15.7psi to about 348psi, alternatively, operate to the pressure of about 290psi from about 85psi.Destilling tower 126 can be configured to and/or be designed and sized to the separation of the gas (such as, flash vapor stream) providing proper volume.As read of the present disclosure those skilled in the art will recognize that, the air-flow 26 of process or air-flow 18 can retain and/or remain in any reasonable time amount in destilling tower 126, such as, provide the time quantum that the component of fully separation destilling tower 126 is required.

In embodiments, air-flow 26 or the air-flow 18 of process can be introduced into destilling tower 126 and without compression step, that is, at the air-flow 26 of process or air-flow 18 from after separator 108 sends and air-flow 26 or the air-flow 18 of process need not be compressed before introducing destilling tower 126.In another embodiment, air-flow 26 or the air-flow 18 of process can under the pressure substantially the same with the outlet pressure of separator 108 (such as, be from about 14.7psia to about 527.9psia at the outlet pressure of flash chamber 130, alternatively, from about 15.7psia to about 348psia, alternatively, from about 85psia to about 290psia) be introduced into destilling tower 126.In still another embodiment, air-flow 26 or the air-flow 18 of process can be introduced into destilling tower 126, and do not have obvious compression step.In embodiments, air-flow 26 or the air-flow 18 of process can introduce destilling tower 126 under the pressure of following ranges: be about 25psi from the pressure that separator 108 sends and be about 25psi from being less than air-flow 18 to being greater than the pressure that air-flow 18 sends from separator 108, alternatively, be about 15psi from the pressure that separator 108 sends and be about 15psi from being less than air-flow 18 to being greater than the pressure that air-flow 18 sends from separator 108, alternatively, be about 5psi from the pressure that separator 108 sends and be about 5psi from being less than air-flow 18 to being greater than the pressure that air-flow 18 sends from separator 108.In embodiments, the air-flow 26 of process or air-flow 18 can introduce destilling tower 126 under following ranges pressure: from about 14.7psia to about 527.8psia, alternatively, from about 15.7psia to about 348psia, from about 85psia to about 290psia.

In embodiments, the configurable and/or operation of destilling tower 126 makes middle hydrocarbon stream 29, distillation bottom stream 43 and optional effluent 45 each comprise the expectation part of the component of the air-flow 26 of air-flow 18 or process, number or subset.Such as, as those skilled in the art will recognize that under help of the present disclosure, the position of concrete flow export, the operating parameter of destilling tower 126, the air-flow 26 of process or the composition of air-flow 18 or its combination can be made given stream can comprise one or more components of the air-flow 26 of process or the concrete of air-flow 18 by manipulation.

In the embodiment of the system 200 of Fig. 2 display, middle hydrocarbon stream 29 can be separated in destilling tower 124, to form lightweight hydrocarbon stream 25, to distill bottom stream 33 and optionally effluent 31.Lightweight hydrocarbon stream 25 can comprise ethene, ethane, optionally hydrogen or its combination.Distillation bottom stream 33 can comprise iso-butane.Effluent 31 can comprise iso-butane.The iso-butane of distillation bottom stream 33 can comprise the iso-butane with effluent 31 different stage.Such as, distillation bottom stream 33 can comprise the iso-butane being substantially free of alkene, and effluent 31 can comprise secondary recycle isobutane, and it can comprise alkene.

At least one gas component can send from destilling tower 124 with lightweight hydrocarbon stream 25, and other gas components can send from destilling tower 124 to distill bottom stream 33.Ethene can be comprised from the destilling tower 124 of Fig. 2 with at least one gas component that lightweight hydrocarbon stream 25 sends and other lighter-than-air gas (such as, ethene, ethane, methane, carbon dioxide, nitrogen, hydrogen or its combination) can be comprised further.Such as, ethene can by the total weight of lightweight hydrocarbon stream 25 with from about 50% to about 99%, and alternatively from about 60% to about 98%, alternatively, be present in lightweight hydrocarbon stream 25 from the amount of about 70% to about 95%.

Propylene, propane, butane, iso-butane, pentane, hexane, hexene-1, heavy hydrocarbon or its combination can be comprised with other gas components of distilling bottom stream 33 and sending from destilling tower 124.In embodiments, distillation bottom stream 33 can be free of alkene, alternatively, is substantially free of alkene, alternatively, fundamentally not containing alkene.Such as, alkene by the total weight of distillation bottom stream 33 to be less than about 1.0%, alternatively, can be less than about 0.5%, and alternatively, the amount being less than about 0.1% is present in distillation bottom stream 33.In embodiments, comprise iso-butane, the effluent 31 be made up of iso-butane alternatively can send from destilling tower 124 with effluent 31.

In embodiments, effluent 31 or at least partially distill bottom stream 33 can be recycled.Make effluent 31 or distill bottom stream 33 recirculation at least partially to comprise, such as, through suitable pump or compressor, send effluent 31 or at least partially distill bottom stream 33 return PEP system 200 and/or by effluent 31 or at least partially distill bottom stream 33 introduce PEP system 200, such as, for reusing in the polymerization.In embodiments, effluent 31 or distill bottom stream 33 at least partially can in conjunction with various other components (catalyst, co-catalyst etc.), to form the catalyst slurry that can be introduced into one or more reactors 104,106.Do not intend being limited by theory, because distill bottom stream 33 at least partially can be free of alkene and can iso-butane be comprised, distillation bottom stream 33 can with catalyst component (such as, catalyst, co-catalyst etc.) mixing, and there is no the risk of unexpected polymerisation (such as, being introduced into the pre-polymerization of one or more reactor).So, distillation bottom stream 33 can be used as the source not containing the iso-butane of alkene for polymerisation at least partially.Make effluent 31 or distill bottom stream 33 recirculation at least partially can provide effective and/or cost effectively supplies the means that iso-butane operates for polymerisation process.In alternative embodiments, effluent 31 can be sent or distill bottom stream 33 at least partially to store, for using in the polymerization subsequently or adopting in the method that any other is suitable.

In embodiments, at least partially effluent 31 or at least partially distill bottom stream 33 can return destilling tower 124.Such as, can effluent 31 be sent through reboiler or distill bottom stream 33 to destilling tower 124 at least partially, for other process.

Destilling tower 124 can be configured to and/or be designed and sized to the separation of the gas (such as, the lightweight hydrocarbon stream 25 of Fig. 2) providing proper volume.Such as, destilling tower 124 can in scope from about 50 DEG C to about 20 DEG C, alternatively, from about 40 DEG C to about 10 DEG C, alternatively, the temperature of from about 30 to about 5 DEG C, with in scope from about 14.7psia to about 529.7psia, alternatively, from about 15.7psia to about 348psia, alternatively, operate to the pressure of about 290psia from about 85psia.Destilling tower 124 can be configured to and/or be designed and sized to the separation of the air-flow 26 of the air-flow 18 or process providing proper volume.As the skilled person will recognize, the air-flow 26 of process or air-flow 18 can retain and/or remain in any reasonable time amount in destilling tower 124, and the component as the air-flow 26 or air-flow 18 that can provide abundant separating treatment is required.In embodiments, destilling tower 124 can be equipped with at least two outlets.

In embodiments, the configurable and/or operation of destilling tower 124, each expectation part, number or the subset comprising the air-flow 26 of process or the component of air-flow 18 making the lightweight hydrocarbon stream 25 of Fig. 2 and distillation bottom stream 33.Such as, as those skilled in the art will recognize that under help of the present disclosure, the position of concrete inflow entrance or outlet, the operating parameter of destilling tower 124, the air-flow 26 of process or the composition of air-flow 18 or its combination can be made given stream can comprise one or more components of the air-flow 26 of process or the concrete of air-flow 18 by manipulation.

In optional and/or other embodiment, can comprise from flow separation at least one gas component and make air-flow and absorbent (such as, lyosoption system, as disclosed herein) contact, such as, to make gas component be absorbed by absorbent.In this embodiment, comprise from flow separation at least one gas component and optionally absorb at least one gas component from air-flow.In this embodiment, generally comprise from air-flow absorption at least one gas component and air-flow is contacted with suitable absorbent, at least one component is absorbed by absorbent, and optionally, removes the waste stream comprising unabsorbed gas.In other embodiment, the gas component absorbed from absorbent release can be comprised further from flow separation at least one gas component.

In embodiments, make air-flow contact with absorbent and can comprise any suitable means guaranteeing fully to contact between air-flow and absorbent.The non-limitative example of the suitable means of fully contact is provided between air-flow and absorbent to comprise the use of various reactor assembly such as those disclosed (such as, absorption tower or spraying or blending tank) above.Do not intend being limited by theory, suitable reactor assembly by deposit each other in case stir or mixing two components, circulation, dispersions make the first composition diffuse through the second composition or in the second composition diffusion or various other technologies well known by persons skilled in the art can guarantee two or more gaseous states, liquid and or solid composite between contact.In embodiments, air-flow can contact with suitable ratio with absorbent.The scope of this air-flow and the suitable ratio of absorbent can from about 1,000lb/hr:1000gpm to about 2,500lb/hr:25gpm, alternatively, from about 1000lb/hr:250gpm to about 2500lb/hr:100gpm, alternatively, and about 1875lbs/hr:250gpm.

As Fig. 1-5 in the embodiment of explaining, can comprise from air-flow (such as, m-air-flow 19 in the air-flow 26 of the air-flow 18 of Fig. 1 or the process of Fig. 2 or Fig. 3-5) separating at least one gas component and send air-flow to absorption reactor thermally 116.In one or more embodiments disclosed herein, absorption reactor thermally 116 can comprise reactor, and it is configured to optionally absorb at least the first chemical constituent or compound from the stream comprising the first chemical constituent or compound and one or more other chemical constituent, compounds etc.The non-limitative example of suitable absorption reactor thermally and/or absorption reactor thermally configuration comprises absorption (distillation) tower, pressure swing absorption (PSA) structure, aerosol can, stirring reactor, one or more compressor, one or more recirculation pump or its combination.

In embodiments, absorption reactor thermally can be configured to by gas dissipation in a liquid (such as, by making gas be bubbled through liquid).Such as, in embodiments, absorption reactor thermally 116 can comprise solvent circulation, and it is configured to make solvent cycle through absorption reactor thermally 116.Solvent rate of circulating flow can be determined by the operating condition of absorption system, as following public herein.In embodiments, absorption reactor thermally 116 can comprise one or more pump and/or be communicated with one or more pump fluid, and described pump is configured to solvent is recycled through absorption reactor thermally 116 and/or in absorption reactor thermally 116.In other and/or optional embodiment, absorption reactor thermally 116 can comprise packed bed or post, it is configured to such as, maintain less bubble size (such as, the bubble size of dissipation gas in a liquid), such as, to maintain the relative large surface area of gas and the Contact of liquid, such as, to maintain the efficiency that gas transfer and/or absorption enter liquid.In embodiments, the packing material of packed bed or post can comprise polymeric material, metal material or its combination.In embodiments, absorption reactor thermally 116 can have multiple packed bed or post.In embodiments, only a part of absorption reactor thermally 116 can have packing material.In embodiments, the packing material of the absorption reactor thermally 116 of filling can have random filling and maybe can have structurized filling.The example of suitable absorption reactor thermally is illustrated in gas processer association, " through engineering approaches data book " the tenth edition (Gas Processors Association, " Engineering Data Book " 10 ^thed), Figure 19-16.

Comprise in the embodiment of solvent reaction device at absorption reactor thermally 116, absorption reactor thermally can comprise suitable lyosoption system, as disclosed herein.This absorption reactor thermally 116 can be configured to and keeps lyosoption system.Such as, lyosoption system can be used as liquid, keeps in the reactor as fixed bed or as fluid bed.

In embodiments, suitable lyosoption system can reversibly with ethene and/or iso-butane complexing.This lyosoption system can generally comprise complexing agent and solvent.In embodiments, lyosoption system can be characterized by has selective to ethane of ethene, wherein ethene and ethane in the identical point of pressure of about 14psi with about 40:1, identical point of about 20psi pressure with about 12:1, identical point of about 40psi pressure with about 6:1, exist with about 3:1 with the identical point of pressure at about 180psi.In embodiments, solvent system can be characterized by further there is the tolerance of high pollutant and increase and/or show high stability under the temperature of variation and/or pressure or its combination.

In embodiments, complexing agent can comprise slaine.In this embodiment, slaine can comprise the salt of one or more transition metal and weak ion halogen.The non-limitative example of suitable transition metal comprises silver, gold, copper, platinum, palladium or nickel.The non-limitative example of suitable weak ion halogen comprises chlorine and bromine.In embodiments, suitable transition metal salt can be characterized by the high specific had alkene.The non-limitative example of suitable transition metal-haloid comprises silver chlorate (AgCl) and copper chloride (CuCl).In a particular embodiment, the salt adopted in lyosoption system comprises CuCl.Without wanting to be limited by theory, this slaine can interact with two carbon bonds of alkene (such as, ethene).

In embodiments, complexing agent can comprise copper carboxylate (I).In this embodiment, suitable copper carboxylate (I) can comprise copper (I) and comprise the monocarboxylic acid of 1-20 carbon atom, dicarboxylic acids and/or tricarboxylic salt.The carboxyl acid component of salt can comprise aliphatic character, ring-type composition, aryl elements or its combination.Other suitable examples of copper carboxylate (I) comprise formic acid Cu (I), acetic acid Cu (I), propionic acid Cu (I), butyric acid Cu (I), valeric acid Cu (I), caproic acid Cu (I), sad Cu (I), capric acid Cu (I), 2-ethyl-hexanoic Cu (I), palmitic acid Cu (I), tetradecylic acid Cu (I), toluic acid Cu (I), ethyl acetic acid Cu (I), n-pro-pyl acetic acid Cu (I), normal-butyl acetic acid Cu (I), propionic acid ethyl copper Cu (I), cupric octoate Cu (I), benzoic acid Cu (I), p-p t butylbenzoic acid Cu (I) and analog.In other embodiment, complexing agent can comprise the adduct of copper carboxylate (I), such as, as disclosed herein, and boron trifluoride (BF ₃) adduct.

In other and/or optional embodiment, complexing agent can comprise sulfonic acid copper (I).The non-limitative example of suitable sulfonic acid copper (I) comprises copper (I) salt of the sulfonic acid with 4 to 22 carbon atoms.The sulfonic acid component of salt can comprise aliphatic character, ring-type composition, aryl elements or its combination.Aliphatic sulfonic can be straight chain or side chain.The example of suitable aliphatic sulfonic includes but not limited to n-butanesulfonic acid, 2-ethyl-1-hexane sulfonic acid, 2-methylnonane sulfonic acid, dodecane sulfonic acid, 2-ethyl-5-n-pentyl tridecane sulfonic acid, n-eicosane sulfonic acid and analog.The example of suitable aromatic sulfonic acid comprises benzene sulfonic acid, alkyl benzene sulphonate, wherein moieties comprises 1 to 16 carbon atom, such as p-methyl benzenesulfonic acid, DBSA (adjacent, and to), p-cetyl benzenesulfonic acid and analog, naphthalene sulfonic acids, phenolsulfonic acid, naphtholsulfonic acid and halogeno-benzene sulfonic acid, such as p-chlorobenzenesulfonic acid, p-bromo-benzene sulfonic acid and analog.

In embodiments, complexing agent can comprise hindered olefins further.Such as, in embodiments, complexing agent can comprise such hindered olefins, and its complexing agent forms the copper complex with insufficient solubility.The example of this hindered olefins is propylene tetramer (i.e. laurylene).Do not intend being limited by theory, hindered olefins can increase copper complex formazan solubility and easily be replaced by ethene simultaneously.

In various embodiments, complexing agent can comprise U.S. Patent number 5, and 104,570; 5,191,153; 5,259,986; With 5,523, one or more complexing agents disclosed in 512, its each section is incorporated to herein with its entirety by reference.

In embodiments, solvent can comprise amine or amine complex, aromatic hydrocarbon, alkene or its combination.The non-limitative example of solvent amine comprises pyridine, benzylamine and aniline.Such as, amine can comprise aniline (phenyl amine, aminobenzene); Alternatively, the aniline combined with dimethyl formamide (DMF), and in embodiments, aniline and 1-METHYLPYRROLIDONE (NMP).Solvent comprises in the embodiment of aromatic hydrocarbon wherein, and aromatic hydrocarbon can comprise aryl that is unsubstituted or alkyl replacement.In this embodiment, aromatic hydrocarbon can be in liquid phase under ambient environment.Suitable non-limitative example comprises toluene, dimethylbenzene etc.Solvent comprises in the embodiment of alkene wherein, and non-limitative example comprises the alkene with 10 to 16 carbon atoms.Such as, alkene can comprise propylene tetramer, laurylene, tetradecene, hexadecylene or its combination.

In embodiments, solvent can be characterized by sprotic, that is, do not comprise dissociable hydrogen atom.Do not intend being limited by theory, dissociable hydrogen solvent can cause the double bond hydrogenation in alkene such as ethene between carbon.In addition, solvent can be characterized by polarity, there is slight polarity or there is unidirectional electric charge.Do not intend being bound by theory, polar solvent can interact with salt and at least partly salt be dissolved.

In embodiments, solvent can be characterized by with the industrial production of relative large volume, the liquid with relatively low cost, easily transport or its combination.Solvent can be characterized by the alkene-slaine that can keep complexing or the slaine keeping weak ion further, and no matter how are temperature and/or pressure oscillation.

In embodiments, lyosoption system can comprise copper chloride, aniline and dimethyl formamide (CuCl/ aniline/DMF).In alternative embodiments, lyosoption system can comprise copper chloride, aniline and 1-METHYLPYRROLIDONE (CuCl/ aniline/NMP).In this embodiment, CuCl/ aniline/nmp solvent system can be characterized by the volatilization stability at the temperature of lower pressure and Geng Gao with increase.In alternative embodiments, lyosoption system can comprise copper carboxylate (I) and arsol such as toluene or dimethylbenzene.In alternative embodiments, lyosoption system can comprise sulfonic acid copper (I) and arsol such as toluene or dimethylbenzene.In alternative embodiments, lyosoption system can comprise copper carboxylate (I) and BF in arsol such as toluene or dimethylbenzene ₃adduct.

In embodiments, lyosoption system can comprise 2-ethyl-hexanoic copper (I) and propylene tetramer.In embodiments, lyosoption system can comprise 2-ethyl-hexanoic copper (I) and laurylene.In embodiments, lyosoption system can comprise copper palmitate (I) and hexadecylene.In embodiments, lyosoption system can comprise tetradecylic acid copper (I) and tetradecene.

In embodiments, make at least one component by absorbent absorb can comprise at least one component such as reversibly being combined through forming various bonding, key, attraction, complex compound or its combination, connecting, bonding or its be incorporated into absorbent or its part.Such as, absorbent comprises lyosoption system (such as wherein, CuCl/ aniline/DMF solvent system or CuCl/ aniline/nmp solvent system) embodiment in, absorption at least one component can be comprised make to form complex compound between absorbent and at least one component, be called absorbent components complex compound (such as, the alkene complex of absorption).

Make to absorb at least one component can comprise further provide and/or keep the suitable pressure of air-flow and absorbent contact environment, provide and/or keep the suitable dividing potential drop of gas, the proper temperature providing and/or keep air-flow and absorbent contact environment, catalytic absorption or its combination.Do not intend being limited by theory, absorbent absorbs at least one component can be improved at suitable temperature and/or pressure.

In embodiments, absorption reactor thermally 116 can selective induction heat and/or pressure oscillation, change or circulation.In embodiments, absorption reactor thermally 116 can be configured to from comprising other gases various (such as, ethane, optionally hydrogen) composition optionally absorb and/or induce absorb unreacted vinyl monomer (with optionally, comonomer).In another embodiment, absorption reactor thermally 116 can be configured to optionally to absorb from the composition comprising other gases various and/or induce and absorbs butane, especially iso-butane.In still another embodiment, the composition that absorption reactor thermally 116 can be configured to from comprising other gases various (such as, ethane, optionally hydrogen) optionally absorbs both unreacted ethene and butane, especially iso-butane.

In embodiments, absorption reactor thermally 116 can be configured to provides or maintains suitable temperature, such as, can be depending on the phase that absorption reactor thermally operated in preset time.Such as, absorption reactor thermally 116 can be configured to provides or maintains suitable temperature, such as, for increasing absorb expect chemical species, reduce absorb expect chemical species, from the unabsorbed gas of reactor 116 flash distillation, the object that reclaims unreacted ethene from absorption reactor thermally 116, make absorbent regeneration absorption reactor thermally 116 or its combination.In embodiments, this suitable temperature range can from about 40 ℉ to about 110 ℉, alternatively, from about 40 ℉ to about 60 ℉, alternatively, from about 45 ℉ to about 55 ℉, alternatively, from about 50 ℉ to about 55 ℉, and about 50 ℉ alternatively.Such as, have been found that temperature range is from about 40 ℉ to about 110 ℉, alternatively, from about 40 ℉ to about 60 ℉, the beat all increase that can produce ethylene absorption relative to ethane absorption of the operating temperature of the absorption reactor thermally 116 (with lyosoption system) of about 50 ℉ alternatively.Do not intend being limited by theory, those skilled in the art will recognize that (such as, based on the dividing potential drop concept from Raoult's law) expection ethene and ethane solubility in absorbent solvent at the temperature reduced gradually increases.But expect contrary therewith, find along with when being reduced to 50 ℉ at temperature, the ethene amount absorbed in the absorbent solvent and/or absorbent solvent system of disclosed embodiment reduces.Because this beat all phenomenon, the absorption of ethene can in scope from about 40 ℉ to about 110 ℉, alternatively, in scope from about 40 ℉ to the temperature of about 60 ℉, alternatively, maximum at the temperature of about 50 ℉.Figure 11 is the figure showing ethene and the solubility of ethane in copper chloride, aniline, NMP absorbent solvent system at different temperatures.This figure is illustrated in the solubility trend of expection and the beat all solubility trend of ethene of ethane under the temperature range of above-mentioned discussion.

In embodiments, one or more components (such as, ethene and/or iso-butane) period that absorption reactor thermally 116 can be configured to absorbing air-flow provides or maintains the proper temperature from about 40 ℉ to the scope of about 110 ℉.As above, disclosed in, have been found that ethylene dissolution degree is unexpectedly maximum to the temperature of about 60 ℉ from about 40 ℉ in scope.In embodiments, during absorbing ethene and/or isobutene from air-flow, absorption reactor thermally 116 can from about 40 ℉ to the temperature of about 60 ℉, operate at the temperature of about 50 ℉ alternatively.In alternative embodiments, during absorbing ethene and/or isobutene from air-flow, absorption reactor thermally from about 60 ℉ to about 110 ℉, or can operate to the temperature of about 90 ℉ from about 70 ℉.Such as, this absorption temperature of absorption reactor thermally 116 can suitably as the economic alternative scheme operating (it may require the energy expenditure such as cooled) at lower temperatures.Such as, in scope from about 60 ℉ to about 110 ℉, or to the temperature of about 90 ℉, operate absorption reactor thermally from about 70 ℉, as absorption reactor thermally 116 requires less energy by making absorption reactor thermally operate under the environment temperature in given geographical position, it can produce cost savings.

In embodiments, absorption reactor thermally 116 can be configured to provides or maintains suitable pressure during operation.The scope of this suitable pressure can from about 5psig to about 500psig, alternatively, from about 50psig to about 450psig, alternatively, from about 75psig to about 400psig.In other embodiment, absorption reactor thermally 116 can be configured to provides or maintains suitable ethylene partial pressure during operation.The scope of this suitable ethylene partial pressure can from about 1psia to about 400psia, alternatively, from about 30psia to about 200psia, alternatively, from about 40psia to about 250psia, alternatively, from about 40psia to about 75psia, alternatively, from about 40psig to about 60psig, about 40psig alternatively, alternatively, about 60psig.Do not intend being limited by theory, make absorption reactor thermally 116 supercharging can be beneficial to the complex compound absorbing ethene and/or formation ethene and lyosoption system (such as, CuCl/ aniline/NMP system).And do not intend being bound by theory, along with the pressure drop of absorption reactor thermally, lyosoption system increases the selective of ethene.

In embodiments, absorption reactor thermally 116 can be configured to in batches and/or continuation method.Such as, in embodiments, PEP system can comprise two or more absorption reactor thermallies (such as, such as absorption reactor thermally 116), and it is each can be configured to for batch operation.Such as, by adopting two or more absorption reactor thermallies, this system can be configured to and allows by air-flow component being absorbed to the continued operation for the preparation of " second batch " that absorb in the second absorption reactor thermally simultaneously of " first batch " in the first absorption reactor thermally.So, by circulating between the reactor that two or more are suitable, system can continued operation.

Such as, in embodiments, two or more absorption reactor thermallies (such as, absorption reactor thermally system) can be configured to use liquid flux, such as, lyosoption system disclosed herein or lyosoption carry out the pressure swing absorption (PSA) of ethene.In this embodiment, absorption reactor thermally 116 can comprise two or more absorption reactor thermallies, and it is configured to for PSA (such as, absorption reactor thermally system).Figure 10, display absorption reactor thermally system 1000, has four absorption reactor thermallies 1010,1020,1030 and 1040, is configured to for PSA.Although the embodiment diagram of Figure 10 four absorption reactor thermallies (such as, absorption reactor thermally 1010,1020,1030 and 1040), those skilled in the art, will recognize when reading the disclosure and can adopt two, three, five, six, seven, eight or more individual absorption reactor thermallies similarly.In this embodiment, each absorption reactor thermally can configure substantially as disclosed herein.In embodiments, one or more reactor 1010,1020,1030 and 1040 can through the circulatory system (such as, comprising one or more pump, valve, conduit etc.) connect with between absorption phase in reactor 1010,1020,1030 and 1040 circulating fluid solvent.Absorption reactor thermally 1010,1020,1030 and 1040 can in absorption stage (wherein gas component, such as ethene and/or iso-butane, by lyosoption and/or lyosoption Systemic absorption) and regeneration stage (gas component that is that wherein absorb and/or complexing from lyosoption system and/or lyosoption system release, preparation is reused, as disclosed herein) between circulation.Such as, reactor 1010,1020,1030 and 1040 tunable ground at absorption stage and regeneration stage (such as, through one or more interstage) between circulation, thus not all reactor 1010,1020,1030,1040 all carries out absorbing or regenerating simultaneously.Absorption reactor thermally 1010,1020,1030 and 1040 is configured to in the embodiment of PSA operation wherein, and reactor 1010,1020,1030 and 1040 had both been used as absorber and has also been used as regenerator.In this embodiment, the separation container possibility for regenerating optional (such as, as disclosed herein).

As the example of the PSA operation coordinated, in the given stage during this kind of operation, reactor 1010 can operate with the absorption stage, such as, under acceptance condition as disclosed herein.In the substantially the same time, reactor 1020 can be pressurized to intermediate pressure, such as, lower than absorption pressure.And in the substantially the same time, reactor 1030 can from middle pressure to regeneration pressure, and simultaneous reactions device 1040 can from absorption pressure (from before be in the absorption stage) be decompressed to intermediate pressure.Do not intend being limited by theory, after absorption, the decompression of each reactor 1010,1020,1030 and/or 1040 (such as, from absorption pressure to intermediate pressure with from intermediate pressure to regeneration pressure) gas component of absorption can be made (such as, ethene and/or iso-butane) from absorbent release and/or absorbent regeneration (such as, preparation is used for reusing, as disclosed herein).In embodiments, the pressure from one or more reactor (such as, reactor 1010,1020,1030 and/or 1040) can be used for another pressurization making these reactors.Such as, in the embodiment of Figure 10, in reactor 1040, the pressure of gas can be used for making reactor 1020 be forced into intermediate pressure by pipeline 1050, and valve 1058 and 1084 is in an open position and valve 1082 and 1056 is in the closed position.Valve 1062,1064,1066 and 1068 can be changed between open and closed positions, flows into and outflow reactor 1010,1020,1030 and 1040 to make the Nitrogen in Products in stream 1060.Valve 1052,1054,1056 and 1058 can be changed between open and closed positions, is pressurizeed to make reactor 1010,1020,1030 and 1040 and is reduced pressure by stream 1050.Valve 1082,1084,1086 and 1088 can be changed between open and closed positions, is fed to reactor 1010,1020,1030 and 1040 to make light gas stream 1080 when in the absorption stage.Valve 1092,1094,1096 and 1098 can be changed between open and closed positions, to remove any purge gas from reactor 1010,1020,1030 and 1040 by stream 1090.

In embodiments, during regeneration stage, stripping gas, such as iso-butane or nitrogen, such as, can be added into absorption reactor thermally 1010,1020,1030 and 1040 by flowing 1070.Stream 1070 can be positioned at the bottom of reactor 1010,1020,1030 and 1040, so stripping gas can be bubbled through reactor 1010,1020,1030 or 1040 (and by any packing material wherein).Valve 1072,1074,1076 and 1078 can be changed between the open and closed positions, to add desorption gas to reactor 1010,1020,1030 and 1040 at regeneration period.Do not intend being limited by theory, regeneration period stripping gas can reduce the dividing potential drop of the ethene in absorption reactor thermally 1010,1020,1030 and 1040.

In embodiments, one or more absorption reactor thermally 1010,1020,1030 and 1040 can comprise internals, to prevent channel by liquid absorption solvent distributing gas.Suitable internals can comprise distillation and fill, its distributing gas and reduce the axial backmixing of liquid.Internals can prevent the liquid absorption solvent in absorption reactor thermally 1010,1020,1030 and 1040 mix thus solvent flowing will first saturated and then saturation front (saturation front) move vertically upward by absorption reactor thermally 1010,1020,1030 and 1040.

In embodiments, removal waste stream is comprised from flow separation at least one gas component.In embodiments, residual unabsorbed flow groups divides formation waste stream.The embodiment comprising ethene and absorbent in absorbent components comprises CuCl/ aniline/DMF or CuCl/ aniline/nmp solvent system, and this waste stream can comprise hydrogen, methane, ethane, acetylene, propylene, other hydrocarbon various, volatile contaminant or its combination.In addition, this waste stream can be substantially free of unreacted vinyl monomer or, optionally, comonomer.As used herein, " be substantially free of unreacted vinyl monomer " and be meant to waste gas to comprise and be less than 50% unreacted vinyl monomer by the total weight of this stream, alternatively, be less than 10% unreacted vinyl monomer, alternatively, be less than 1.0% unreacted vinyl monomer, alternatively, be less than 0.1% unreacted vinyl monomer, alternatively, be less than 0.01% unreacted vinyl monomer.

In embodiments, remove waste stream and can comprise cooling waste stream, and/or reduce or increase the pressure of waste stream, make waste stream flow to treatment facility 114.Such as, in embodiments, waste stream by under sufficient pressure, under speed or the suitable sweep gas of its combined traffic (such as, inertia or unreacted gas, as above disclosed) by comprising the container (such as, absorption reactor thermally 116) of waste gas with the quilt " cleaning " from its combustion gas.Such as, in the embodiment of explaining in figs. 1-5, produce from flow separation at least one gas component and be substantially free of unreacted vinyl monomer (optionally, comonomer) waste gas streams 20, alternatively, there is the waste gas streams of the unreacted vinyl monomer (optionally, comonomer) reducing concentration.Such as, waste gas streams can comprise and be less than about 30% by the total weight of this stream, alternatively, is less than about 25%, alternatively, is less than about 20%, alternatively, is less than about 15%, alternatively, is less than the unreacted vinyl monomer of about 10%.In other embodiment, ethene can reduce the percentage of the ethene existed in air-flow before flow separation at least one gas component.Such as, waste gas streams can comprise and be less than about 40% by the total weight of this stream, alternatively, is less than about 30%, alternatively, and the unreacted vinyl monomer existed in air-flow before being less than the separation of about 20%.

In embodiments, the gas component (such as, absorption reactor thermally 116 situ and/or in another container of such as regenerator 120) absorbed from absorbent release can be comprised further from flow separation at least one gas component.The gas component absorbed from absorbent release generally comprises any suitable means: its reverse combined by its at least one gas component, connect, bonding or its be incorporated into the various bondings of absorbent or its part, key, attraction, complex compound or its combination.The non-limitative example of the suitable means of the gas component absorbed by its release comprises the absorption dynamics or absorption equilibrium, heating or decompression absorbent, the dividing potential drop changing the gas absorbed or its combination that change absorbent.

In embodiments, in regeneration and/or desorption phase, the gas component of absorption can discharge from the absorbent in one or more this absorption reactor thermally (such as, desorb and/or solution complexing).In embodiments, regeneration stage can comprise and makes lyosoption system regeneration to produce unreacted ethene; In embodiments, regeneration stage can comprise the lyosoption system regeneration made in absorption reactor thermally 116, to produce unreacted ethene.Such as, in the embodiment of Fig. 1 and 2 (and/or, absorption reactor thermally 116 is configured in the embodiment of PSA structure wherein, as herein disclosed in reference Figure 10), absorption reactor thermally 116 can be configured to air release gas that is that induction absorbs from lyosoption or complexing (such as, that absorb and/or the ethene of complexing and/or the desorb of iso-butane and/or separate complexing), as herein in detail disclosed in.Do not intend being limited by theory, the release of gas that is that induction absorbs or complexing can comprise the kinetics that changes lyosoption system or gas-solvent balance, the temperature of absorption reactor thermally 116, the pressure of absorption reactor thermally 116, the dividing potential drop of the gas of absorption or its combination.In this embodiment, absorption reactor thermally 116 can comprise be configured to change kinetics, gas-solvent balance, the temperature of absorption reactor thermally 116, the pressure of absorption reactor thermally 116 or its combination controller, heat pipe, conductivity cell, compressor, vavuum pump etc. or its combine.

Such as, in embodiments, the gas component that release absorbs can comprise the solution decompression of the ethene making to comprise complexing to suitable dividing potential drop.In other embodiment, the gas component that release absorbs can comprise heating absorption reactor thermally 116 (alternatively, in regenerator 120, as following public) herein and comprise the solution of the ethene of complexing to suitable temperature.This suitable temperature range can from about 110 ℉ to about 200 ℉, alternatively, from about 140 ℉ to about 160 ℉, alternatively, from about 160 ℉ to about 200 ℉, alternatively, from about 180 ℉ to about 200 ℉, discharge from lyosoption with penetration enhancement compound (such as, ethene and/or iso-butane).Such as, in a particular embodiment, in absorbent components (such as, ethene and/or isobutene) from lyosoption deenergized period, absorption reactor thermally 116 (alternatively, regenerator 120) from about 160 ℉ to about 200 ℉, alternatively, can operate to the temperature of about 200 ℉ from about 180 ℉.In alternative embodiments, in absorbent components (such as, ethene and/or isobutene) from lyosoption deenergized period, absorption reactor thermally 116 (alternatively, regenerator 120) can operate to the temperature of about 160 ℉ from about 140 ℉.Such as, this release temperature can suitably as economic alternative scheme.Such as, at absorbent components deenergized period, operation absorption reactor thermally, as absorption reactor thermally 116 (alternatively, regenerator, as regenerator 120) originate (such as by making to be derived from other to the temperature of about 160 ℉ from about 140 ℉ in scope, heat exchanger, polymer reactor, flash line heater, flash chamber etc. in the heat exchanger of polymer reactor cooling agent, low-pressure stream, regenerator upstream, absorbent recirculation line or its combination) heat need less energy for heating absorption reactor thermally and/or regenerator, it can produce cost savings.

In addition, in this embodiment, absorption reactor thermally 116 can be configured to Exhaust Gas (such as, the gas absorbing before and then discharge, such as ethene) and/or is beneficial to the gas absorbed through pressure reduction release.Absorption reactor thermally 116 can be configured to provides or maintains suitable dividing potential drop.The scope of this suitable dividing potential drop can from about 0.1psig to about 40psig, alternatively, from about 5psig to about 30psig, alternatively, from about 5psig to about 15psig.In embodiments, absorption reactor thermally 116 can be configured to provides or maintains ethylene partial pressure scope from about 0psia to about 5psia.

In alternative embodiments, the solution shifting out the component complex compound (such as, the alkene complex of absorption) comprising absorption can be comprised further from flow separation at least one gas component, for further process.At this optional embodiment, the absorption complex compound comprising the gas component of absorption can be moved to regenerator 120 from absorption reactor thermally 116, for discharging the gas component of absorption and/or making absorption complex compound be regenerated as combined-flow 28.In embodiments, regenerator 120 can make lyosoption system regeneration to produce unreacted ethene; In embodiments, regenerator 120 can make the lyosoption system regeneration in regenerator 120 to produce unreacted ethene.

In this embodiment, combined-flow 28 can comprise ethene, ethane and/or iso-butane.The scope that ethene exists can from about 0.1% to about 10% by the total weight of this stream, alternatively, and from about 0.4% to about 5%, alternatively, from about 0.5% to about 2.5%.The scope that ethane exists can from about 0.1% to about 1% by the total weight of this stream, alternatively, and from about 0.2% to about 0.5%.The scope that iso-butane exists can from about 0.1% to about 1% by the total weight of this stream, alternatively, and from about 0.2% to about 0.5%.

In one or more embodiments disclosed herein, combined-flow is separated into recirculation flow and absorbent stream (such as, at block 92) and comprises the gas component absorbed from absorbent release.As above set forth, the gas component absorbed from absorbent release generally comprises any suitable means, its reverse combined by its at least one gas component, connect, bonding or its be incorporated into the various bondings of absorbent or its part, key, attraction, complex compound or its combination.Various method and/or the parameter of the gas component that release absorbs is disclosed above with reference to the release in absorption reactor thermally.

In the embodiment of Fig. 5 explaination, combined-flow is separated into recirculation flow and absorbent stream and can comprises and send combined-flow 28 to regenerator 120.In one or more embodiments disclosed herein, regenerator 120 can comprise the equipment or the device that are configured to reclaim, regenerate, recycle and/or purify lyosoption and/or discharge the gas absorbed.The non-limitative example of suitable regenerator comprises flashing reactor, Depressor response device, solvent reclamation reactor or its combination.

In embodiments, regenerator 120 can be configured to and operates based on pressure reduction.In this embodiment, regenerator 120 can be configured to provides or maintains suitable interior pressure.This interior pressure scope suitably can from about 0psig to about 150psig, alternatively, from about 5psig to about 30psig, alternatively, from about 5psig to about 15psig, alternatively, from about 0psig to about 10psig.In embodiments, regenerator 120 can be configured to provides or maintains suitable dividing potential drop.This suitable partial pressure range can from about 0psia to about 50psia.

In embodiments, regenerator 120 can be configured to the temperature operation based on raising.This regenerator 120 can be configured to and provides or maintain suitable temperature.This suitable temperature range can from about 110 ℉ to about 200 ℉, alternatively, from about 140 ℉ to about 200 ℉, alternatively, from about 140 ℉ to about 160 ℉, alternatively, from about 160 ℉ to about 200 ℉, alternatively, from about 180 ℉ to about 200 ℉, with the compound (such as, ethene and/or iso-butane) absorbed from lyosoption evaporation and/or release.In embodiments, regenerator 120 (such as, as absorption reactor thermally 116) can use comprise cooling water, low-pressure steam or its combination thermal source carry out heating with desorb or regenerable absorbent solvent system.Cooling water, low-pressure steam or its combination can be suitable for reboiler 120 (or absorption reactor thermally 116, as above disclosed) to from about 140 ℉ to the temperature of about 200 ℉.

In embodiments, regenerator 120 is configurable in batches and/or continuation method.Such as, in embodiments, PEP system can comprise two or more absorption and regeneration devices (such as, the regenerator 1220 and 1222 of such as Figure 12), and it is each configurable for batch operation.As above set forth, by adopting two or more absorption reactor thermallies, this system operable is to make absorbent cyclic regeneration.

In embodiments, combined-flow be separated into absorbent stream---it can reuse in absorption reaction---that recirculation flow and absorbent stream can produce regeneration and comprise unreacted monomer (optionally, comonomer) recirculation flow, it can be reintroduced back to PEP method or reuse in PEP method.Such as, in the embodiment of Fig. 5 explaination, combined-flow 28 is separated into recirculation flow and absorbent stream and produces that recirculation flow 22---it can return such as clarifier 102, and the absorbent stream 30 of regeneration, it can return such as absorption reactor thermally 116.

In embodiments, the gas that release absorbs also can produce and comprise unreacted monomer (optionally, comonomer) recirculation flow, its can return separator 108 for pressurization (such as, through being positioned at one or more compressors at separator 108 place).Such as, in the embodiment that Fig. 1-5 explains, the gas that release absorbs produces recirculation flow 22, and it can return separator 108, and 105.Recirculation flow 22 supercharging can be produced and be reintroduced back to stream (not shown), it can be reintroduced back to PEP method or reuse in PEP method.Such as, in the embodiment that Fig. 1-5 explains, be reintroduced back to stream and can be introduced into clarifier 102.In alternative embodiments, recirculation flow (such as recirculation flow 22) can be pressurized and/or be reintroduced back to PEP method, and do not return separator 108,105.In embodiments, recirculation flow 22 can comprise substantially pure ethene; Alternatively, recirculation flow 22 can comprise ethene and butane, especially iso-butane.In embodiments, air-flow can comprise nitrogen, ethene, ethane and/or iso-butane.The scope that ethene exists can from about 65% to about 99% by the total weight of stream, alternatively, and from about 70% to about 90%, alternatively, about 75% to about 85%.The scope that ethane exists can from about 1% to about 20% by the total weight of stream, alternatively, and from about 5% to about 15%, alternatively, from about 7.5% to about 12.5%.The scope that iso-butane exists can from about 1% to about 20% by the total weight of stream, alternatively, and from about 5% to about 15%, alternatively, from about 7.5% to about 12.5%.

In one or more embodiments disclosed herein, burner exhaust stream (such as, at block 66 or 76) can generally comprise burning or incinerate one or more gas components of waste gas streams 20.In embodiments, burner exhaust stream 20 can comprise the cracking of waste gas streams 20 or combustion product, catalytic cracking, pyrolysis, dehydrogenation, washing, conversion, process or its combination further or alternatively.

As disclosed herein, waste gas streams 20 can comprise the solvent of volatilization, unreacted gas, secondary products, pollutant, hydrocarbon or its combination.In embodiments, waste gas streams 20 can comprise hydrogen, nitrogen, methane, ethene, ethane, propylene, propane, butane, iso-butane, heavy hydrocarbon or its combination.The scope that ethene exists can from about 1% to about 40% by the total weight of stream, alternatively, and from about 2.5% to about 20%.The scope that ethane exists can from about 5% to about 50% by the total weight of stream, alternatively, and from about 30% to about 40%.The scope that iso-butane exists can from about 1% to about 20% by the total weight of stream, alternatively, and from about 1.5% to about 5%, alternatively, from about 2% to about 3%.The scope that nitrogen exists can from about 10% to about 80% by the total weight of stream, alternatively, and from about 35% to about 50%, alternatively, from about 40% to about 45%.

As Fig. 1-5 in the embodiment of explaining, burner exhaust stream can comprise and sends waste gas streams 20 to treatment facility 114.In one or more embodiments disclosed herein, treatment facility 114 can comprise combustion apparatus or device, such as torch.The non-limitative example of suitable torch comprises torch, incinerator etc. or its combination.Torch suitably can comprise one or more controlled nozzle, incendiary source, by-passing valve, pressure relief valve or its combination.Torch can be configured to and is provided for various waste product, such as, and the environment of atomic gas (such as nitrogen, oxygen), oxide (such as carbon monoxide, nitrogen or sulfur oxide), various undesired gaseous products or its combined burning.In embodiments, torch can comprise equipment or device in addition, and it is configured to before combustion, period and/or optionally remove one or more pollutants (such as, making given combustion product not be released into air) afterwards.

In one or more embodiments disclosed herein, treatment facility 114 can comprise such as cracking unit, catalytic cracking unit, washer, converter, treating apparatus, dehydrogenator, degasifier or its combination.In embodiments, treatment facility 114 can comprise ethylene cracker device.In treatment facility 114, from one or more gas components of waste gas streams 20, such as ethane can change into the product of expectation, such as vinyl monomer.The expectation product formed in treatment facility 114 can be recirculated to such as clarifier 102, reactor 104, reactor 106 one or more.

In other optional embodiments, waste gas streams 20 can be used as fuel and (such as produces for steam or common property raw (co-gen) operation, and/or can be used as fuel and/or be fed to thermal cracking unit, to form ethene (such as, to form incoming flow 10).In another optional embodiment, the waste gas from waste gas streams 20 can export monomer unit to from device.

In embodiments, one or more disclosed system (such as, PEP system 100,200,300,400 and/or 500) and/or method is (such as, PEP method 600,700,800 and/or 900) enforcement can make to reclaim most of vinyl monomer, itself otherwise due to the operation of this system or method, such as, lose by burning.In embodiments, one or more disclosed system can make to reclaim total weight by stream up to about 75%, alternatively, up to about 85%, alternatively, up to about 90%, alternatively, up to about 95% otherwise the vinyl monomer that will lose.In embodiments, one or more open system can make to reclaim total weight by stream up to about 75%, alternatively, up to about 85%, alternatively, up to about 90%, alternatively, up to about 95% otherwise the iso-butane that will lose.Reclaim this part unreacted vinyl monomer, such as, by the utilization ratio of improving vinyl monomer with reduce the capital input relevant with acquisition vinyl monomer, significant economic benefit can be produced.Similarly, reclaiming this part iso-butane, such as, by reducing the capital input relevant to obtaining iso-butane and/or the existence by reducing iso-butane in flare discharge, significant economic benefit can be produced.

In embodiments, the enforcement of one or more disclosed system and/or method can reduce and is transferred to the ethane of polymer reactor 106 and/or the amount of hydrogen.In embodiments, the enforcement of one or more disclosed system and/or method can reduce and returns the ethane of polymer reactor (such as reactor 104 and/or 106) and/or the amount of hydrogen through recirculation flow.By reducing the amount of the ethane to polymer reactor comprised in stream, the gross efficiency (such as, by increasing ethylene concentration, and not reaching the bubbling point in loop reactor) of polyethylene production can be improved.Such as, the amount reducing ethane in stream can be improved polymer reactor efficiency, improves catalyst efficiency, reduces Polymeric Soil, reduces the polymerization downtime, improves the production of bimodal polymers type, improve the production of copolymer or its combination.

The various embodiments shown in figure can be simplified and may not explain general device such as heat exchanger, pump and compressor; But technical staff will recognize that disclosed method and system can be included in normally used this device in whole polymers manufacturing.

Technical staff will recognize that industry and commercial polyethylene manufacture method may required one or more usual several compressors or similar devices.This compressor uses in whole polyethylene manufactures, such as, pressurize at polymerization period chien shih reactor 104,106.In addition, technical staff will recognize that preparation method for polythene comprises one or more degasifier and/or similar deoxygenated device, such as purifying solvent or reactant and/or the reactor for cleaning oxygen.Exist in commercial polyethylene manufacturing works because such as provide the foundation structure of power supply and maintenance compressor and/or degasifier and support, these available resources of a reallocation part are for needing seldom in disclosed system---if any---other capital cost is to combine disclosed system and or method.

In addition, because adopted compressor, degasifier and other assemblies various in various polyethylene process and system, the chance increasing the operation of this device can improve the gross efficiency of polyethylene production system and method.Such as, when a part of PEP method or system off-line are used for maintenance and/or repair, the system (such as, compressor, degasifier, reactor etc.) of other parts can continue to provide service according to current method.Operation and/or reallocation resource be used for open PEP system and/or method operation can thus improve the efficiency using conventional system.

Description in addition

Describe the method and system of Component seperation in paradigmatic system.There is provided terms hereinafter as further description:

The method of embodiment A Component seperation in polymer production system, comprising:

Polymerizate stream is separated into air-flow and polymer flow, and wherein air-flow comprises ethane and unreacted ethene;

Airflow distillation is become lightweight hydrocarbon stream, wherein lightweight hydrocarbon stream comprises ethane and unreacted ethene;

Make lightweight hydrocarbon stream and lyosoption system contacts, wherein from the unreacted at least partially ethene of lightweight hydrocarbon stream by lyosoption Systemic absorption; With

From lyosoption system recoveries waste gas streams, wherein waste gas streams comprises ethane, hydrogen or its combination.

The method of embodiment B embodiment A, comprises further:

Make lyosoption system regeneration to produce the ethene reclaimed.

The method of embodiment C embodiment A, comprises further:

Airflow distillation is become to comprise the effluent of iso-butane.

The method of embodiment D embodiment A, comprises further:

Process waste gas streams in processing.

The method of embodiment E embodiment D, wherein treatment facility comprises cracking unit, catalytic cracking unit, washer, converter, treating apparatus, dehydrogenator, degasifier, torch or its combination.

The method of embodiment F embodiment A, wherein absorbent solvent system configuration is operate to the temperature of about 110 ℉ from about 40 ℉ in scope.

The method of embodiment G embodiment A, wherein absorbent solvent system comprises copper chloride, aniline and 1-METHYLPYRROLIDONE.

The method of embodiment H Component seperation in polymer production system, comprising:

Hydrocarbon stream and the first bottom stream in the middle of airflow distillation is become, wherein, hydrocarbon stream comprises ethane, ethene and iso-butane;

Middle hydrocarbon stream is distilled into lightweight hydrocarbon stream and the second bottom stream, wherein lightweight hydrocarbon stream comprises ethane and ethene;

The method of embodiment I embodiment H, comprises further:

Make lyosoption system regeneration to produce the ethene reclaimed.

The method of embodiment J embodiment H, comprises further:

Middle hydrocarbon stream is distilled into the effluent comprising iso-butane, wherein the second bottom stream comprises iso-butane, and wherein the second bottom stream is substantially free of alkene.

The method of embodiment K Component seperation in polymer production system, comprising:

Olefinic monomer is polymerized in the first polymer reactor, with m-polymerizate stream in producing;

By in m-polymerizate stream be separated in m-air-flow and in m-polymer flow, wherein, m-air-flow comprises ethane, unreacted ethene and hydrogen; With

M-polymer flow is polymerized in the second polymer reactor.

The method of embodiment L embodiment K, separating step comprises the pressure of m-polymerizate stream in reduction, so that flash distillation ethene, ethane, hydrogen or its combination.

The method of embodiment M Component seperation in polymer production system, comprising:

Olefinic monomer is polymerized in the first polymer reactor;

By in m-polymerizate stream be separated in m-air-flow and in m-polymer flow, wherein, m-air-flow comprises ethane and unreacted ethene;

M-polymer flow is polymerized in the second polymer reactor; With

Scavenger was introduced before the second polymer reactor.

The method of embodiment N embodiment M, introduced scavenger and comprises m-polymerizate stream in scavenger introducing before the second polymer reactor.

The method of embodiment O embodiment M, wherein scavenger comprises hydrogenation catalyst.

The method of embodiment P embodiment M, wherein separating step comprises:

The pressure of m-polymerizate stream in reduction, so that flash distillation ethene and ethane.

The method of embodiment Q embodiment M, wherein scavenger reduced the concentration of hydrogen before the second polymer reactor.

The method of embodiment R Component seperation in polymer production system, comprising:

Make from the hydrogen at least partially of m-polymerizate stream degassed, to produce the product stream that hydrogen reduces;

By hydrogen reduce product stream be separated in m-air-flow and in m-polymer flow, wherein, m-air-flow comprises ethane and unreacted ethene; With

M-polymer flow is polymerized in the second polymer reactor.

The method of embodiment S embodiment R, separating step comprises the pressure reducing the product stream that hydrogen reduces, so that flash distillation ethene and ethane.

The method of embodiment T embodiment R, wherein, in m-air-flow, the amount of hydrogen accounts for and is less than about 1wt%.

The method of embodiment U embodiment R, comprises further:

M-air-flow and lyosoption system contacts in making, wherein from the unreacted at least partially ethene of m-air-flow by lyosoption Systemic absorption; With

Make lyosoption system regeneration to produce the ethene reclaimed.

The method of embodiment V embodiment R, comprises further:

From lyosoption system recoveries waste gas streams, wherein waste gas streams comprises ethane.

Embodiment

Generally described the disclosure, provide following embodiment as detailed description of the invention of the present disclosure, to show its practice and advantage.Should be understood these provide by the mode of explaination and be not intended to limit description or claims by any way.

Adopt the business method simulator calculated, to export from producing according to the model of system disclosed herein and/or method.In fig. 12, it shows the embodiment of absorption system 1200 as disclosed herein, and is applied to description the following examples in the model explaination adopted.In the embodiment shown in fig. 12, from the polymerizate flow point of polyethylene reactor 104,106 disclosed in the embodiment of the PEP system 100,200,300,400 or 500 at Fig. 1 to 5 from light gas stream 1218 be fed to absorption reactor thermally 1216.Total mole of light gas stream 1218 and mass flow and component molar and mass flow display be in the following Table 1:

Table 1

The unreacted ethene entering absorption reactor thermally 1216 is absorbed in the lyosoption system of absorption reactor thermally 1216.The unreacted ethene absorbed flow to the first regenerator 1220 as combined-flow 1228.In stream 1228, the ethene of absorption is heated by heat exchanger REG1HEAT, then enters the first regenerator 1220.Ethene is from the solvent desorption of the lyosoption system of the first regenerator 1220 and flow through stream 1229 to Second reactivator 1222.Flow 1229 available heat exchanger REG2COOL to cool, then enter Second reactivator 1222.Ethene reclaims in stream 1224.Lyosoption in stream 1232 and 2134 combines to be recycled to absorption reactor thermally 1216 in stream 1230 in heat exchanger FEEDCOOL.

Table 2 shows the operating condition of the embodiment 1-44 of the ethylene recovery of the system 1200 using Figure 12.For the embodiment of display in table 2, lyosoption system comprises copper chloride, aniline and NMP system, and as disclosed herein, and the composition of purified product is based on the ethylene recovery of 90%.The composition of the purified product reclaimed from the stream 1224 of Figure 12 comprises ethene, ethane, nitrogen, hydrogen and iso-butane.The wt% of each of these components of purified product shows in table 2.Discuss the embodiment selected from table 2 below in detail.

Embodiment 3

In the embodiment 3 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 15 ℉, wherein the lean solvent temperature of 14 ℉ and the pressure of 40psig.First regenerator 120 operates at the temperature of 150 ℉ and the pressure of 0psig.Second reactivator 122 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, system 900 reclaims ethene and the solvent rate of circulating flow to 344 of 90%, the amount to 64.5% of ethene in 776lb/hr and purified product.

Embodiment 4

In the embodiment 4 of table 2, operating condition is identical with embodiment 3, operates at the temperature of 200 ℉ and the pressure of 0psig unlike the first regenerator 1220.Under these conditions, for the solvent rate of circulating flow of 143,736lb/hr, system 900 reclaims the ethene of 90%, and purified product comprises the ethene of 77.5%.

Embodiment 7

In the embodiment 7 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 53 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 40psig.First regenerator 120 operates at the temperature of 150 ℉ and the pressure of 0psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, for the solvent rate of circulating flow of 53,920lb/hr, system 900 reclaims the ethene of 90%.The purified product composition display of embodiment 7 in table 2.

When comparing embodiment 7 with embodiment 3 and 4 time, in embodiment 7, the solvent rate of circulating flow of 53,920lb/hr to be less than in embodiment 3 and 4 flow velocity of 143,736lb/hr and 344,776lb/hr.Therefore, the embodiment 7 absorption temperature shown for 53 ℉ compares the absorption temperature of 15 ℉, the solvent rate of circulating flow absorbing ethene requirement in copper chloride aniline NMP lyosoption system is more much smaller, this is because ethene in lyosoption system solubility for the beat all decline of temperature lower than about 50 ℉.

Embodiment 8

In the embodiment 8 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 55 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 40psig.First regenerator 1220 operates at the temperature of 200 ℉ and the pressure of 0psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, for the solvent rate of circulating flow of 47,785lb/hr, system 800 reclaims the ethene of 90%.The purified product composition display of embodiment 8 in table 2.

Embodiment 8 to confirm in embodiment 7 result of display, needs lower solvent rate of circulating flow when operating at the temperature of absorption reactor thermally 1216 at the temperature of 55 ℉ instead of lower than 50 ℉.Embodiment 2 additionally shows regenerator 1220 does not affect solvent rate of circulating flow with significance degree from 150 ℉ to 200 ℉ change temperature.

Embodiment 19

In the embodiment 19 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 53 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 40psig.First regenerator 1220 operates at the temperature of 200 ℉ and the pressure of 10psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 10psig.Under these conditions, for the solvent rate of circulating flow of 59,272lb/hr, system 1200 reclaims the ethene of 90%.The display of purified product composition in table 2.

Embodiment 19 confirms the lower solvent circulation rates discussed in embodiment 7 and 8 when comparing with embodiment 3 and 4.Embodiment 19 also shows and changes pressure between 0psig and 10psig in the first and second regenerators 1220 and 1222 and significantly do not change result.The operation of regenerator 1220 and 1222 under 0psig can provide lower solvent circulation rates and the product purity of raising, and the operation of regenerator 1220 and 1222 under 10psig can provide safer design, because the malleation in regenerator 1220 and 1222 reduces the chance of air and water permeation through seepage in system and method, this infiltration can be reacted with the copper chloride in lyosoption system and suppress to carry out.

Embodiment 28

In the embodiment 28 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 52 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 60psig.First regenerator 1220 operates at the temperature of 100 ℉ and the pressure of 0psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, for the solvent rate of circulating flow of 58,613lb/hr, system 1200 reclaims the ethene of 90%.The display of purified product composition in table 2.

Under the condition of embodiment 28, solvent rate of circulating flow is less than the solvent rate of circulating flow of embodiment 3 and 4, and in purified product, the amount of ethene is significantly higher.

Embodiment 29

In the embodiment 29 of table 2, the absorption reactor thermally 1216 in Figure 12 operates under 55 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 60psig.First regenerator 1220 operates at the temperature of 150 ℉ and the pressure of 0psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, for the solvent rate of circulating flow of 51,106lb/hr, system 1200 reclaims the ethene of 90%.The display of purified product composition in table 2.

Under the condition of embodiment 29, solvent rate of circulating flow is less than the solvent rate of circulating flow of embodiment 3 and 4, and in purified product, the amount of ethene is significantly higher.

Embodiment 30

In the embodiment 30 of table 2, the absorption reactor thermally 1216 in Figure 12 operates under 56 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 60psig.First regenerator 1220 operates at the temperature of 200 ℉ and the pressure of 0psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, for the solvent rate of circulating flow of 46,744lb/hr, system 1200 reclaims the ethene of 90%.The display of purified product composition in table 2.

Under the condition of embodiment 30, solvent rate of circulating flow is less than the solvent rate of circulating flow of embodiment 3 and 4, and in purified product, the amount of ethene is significantly higher.

Embodiment 33

In the embodiment 33 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 102 ℉, and wherein lean solvent temperature is 100 ℉.Absorption reactor thermally 1216 also operates under the pressure of 60psig.First regenerator 1220 operates at the temperature of 200 ℉ and the pressure of 0psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 0psig.Under these conditions, for the solvent rate of circulating flow of 63,435lb/hr, system 900 reclaims the ethene of 90%.The purified product composition display of embodiment 33 in table 2.

Under the condition of embodiment 33, solvent rate of circulating flow is less than the solvent rate of circulating flow of embodiment 3 and 4, and in purified product, the amount of ethene is significantly higher.And, embodiment 33 shows absorption reactor thermally 116 and operates at the temperature that the temperature of the maxima solubility shown than dissolubility picture is higher, such as, under 102 ℉ of display in such as embodiment 33, still can prove economic feasibility, because such as, the condition that solvent rate of circulating flow compares embodiment 3 and 4 is still lower.

Embodiment 40

In the embodiment 40 of table 2, the absorption reactor thermally 1216 in Figure 12 operates at the temperature of 52 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 60psig.First regenerator 1220 operates at the temperature of 150 ℉ and the pressure of 10psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 10psig.Under these conditions, for the solvent rate of circulating flow of 57,441lb/hr, system 1200 reclaims the ethene of 90%.The purified product composition display of embodiment 40 in table 2.

Under the condition of embodiment 40, solvent rate of circulating flow is less than the solvent rate of circulating flow of embodiment 3 and 4, and in purified product, the amount of ethene is significantly higher.

Embodiment 41

In the embodiment 41 of table 2, the absorption reactor thermally 1216 in Figure 12 operates under 55 ℉, and wherein lean solvent temperature is 50 ℉.Absorption reactor thermally 1216 also operates under the pressure of 60psig.First regenerator 1220 operates at the temperature of 200 ℉ and the pressure of 10psig.Second reactivator 1222 operates at the temperature of 50 ℉ and the pressure of 10psig.Under these conditions, for the solvent rate of circulating flow of 51,482lb/hr, system 900 reclaims the ethene of 90%.The display of purified product composition in table 2.

Under the condition of embodiment 41, solvent rate of circulating flow is less than the solvent rate of circulating flow of embodiment 3 and 4, and in purified product, the amount of ethene is significantly higher.

Embodiment is simulated

Adopt the business method simulator calculated, to export from producing according to the alternate model of system disclosed herein and/or method.The model adopted is illustrated in Figure 13 place, and wherein the air-flow (such as, light gas stream disclosed herein) of called after VAPFEED is fed to absorption reactor thermally ASORB1.The output produced by business method simulator is material balance and thermally equilibrated, and display in table 3.The stream of explaining in corresponding Figure 10 of name of the various stream of the name enumerated in table 3.In Figure 13, ASORB1 is absorption reactor thermally, and it is shown as the four stage absorbers operated under 90 ℉.

Disclose at least one embodiment, and the modification of the feature (one or more) of the embodiment (one or more) of being made by those skilled in the art and/or embodiment, combination and/or amendment drop in the scope of the present disclosure.The optional embodiment produced by the feature combining, integrate and/or omit embodiment (one or more) is also in the scope of the present disclosure.When clearly expressing number range or boundary, this expression scope or boundary are understood to include the iteration ranges of the same order of magnitude in the scope or boundary that drop on and clearly express or boundary (such as, from about 1 to about 10 comprise 2,3,4 etc.; Be greater than 0.10 and comprise 0.11,0.12,0.13 etc.).Such as, no matter when disclose there is lower limit R _lwith upper limit R _unumber range, specifically disclose any numerical value dropped within the scope of this.In particular, the following numerical value dropped within the scope of this is specifically disclosed: R=R _l+ k* (R _u-R _l), wherein k is the variable of scope from 1% to 100%, 1% increment, that is, k is 1%, 2%, 3%, 4%, 5% ... 50%, 51%, 52% ... 95%, 96%, 97%, 98%, 99% or 100%.And, also specifically disclose any number range of two R numerical definitenesses as defined above.Use term " optionally " to be meant to need this key element or optionally do not need this key element with regard to any key element in claim, two kinds of replacement schemes all fall within the scope of the claims.The use of wider term, such as comprises, comprises and has the term be interpreted as narrower, such as by ... composition, substantially by ... composition, and substantially by ... formation provides support.Therefore, protection domain is not limited by the description of explaining above, but defined by the appended claims, and this scope comprises all equivalents of claim theme.Each and all claims are as being further openly incorporated in description, and claim is the embodiment (one or more) of invention disclosed theme.In the disclosure, the discussion of bibliography does not approve that it is prior art, especially publication date any bibliography after the priority of the application.The all patents quoted in the disclosure, patent application and publication are incorporated to herein by reference, are the degree that the disclosure provides exemplary, procedural or other details are supplemented to them.

Claims

1. the method for Component seperation in polymer production system, comprising:

A. polymerizate stream is separated into air-flow and polymer flow, wherein said air-flow comprises ethane and unreacted ethene;

B. described airflow distillation is become lightweight hydrocarbon stream, wherein said lightweight hydrocarbon stream comprises ethane and unreacted ethene;

C. make described lightweight hydrocarbon stream and lyosoption system contacts, wherein from the described at least partially unreacted ethene of described lightweight hydrocarbon stream by described lyosoption Systemic absorption; With

D. from described lyosoption system recoveries waste gas streams, wherein said waste gas streams comprises ethane, hydrogen or its combination.

2. method according to claim 1, comprises further:

Make described lyosoption system regeneration, to produce the ethene of recovery.

3. the method described in claim 1 to 2, comprises further:

Described airflow distillation is become to comprise the effluent of iso-butane.

4. the method for Component seperation in polymer production system, comprising:

B. hydrocarbon stream and the first bottom stream in the middle of described airflow distillation being become, wherein said middle hydrocarbon stream comprises ethane, ethene and iso-butane;

C. described middle hydrocarbon stream is distilled into lightweight hydrocarbon stream and the second bottom stream, wherein said lightweight hydrocarbon stream comprises ethane and ethene;

D. make described lightweight hydrocarbon stream and lyosoption system contacts, wherein from the unreacted at least partially ethene of described lightweight hydrocarbon stream by described lyosoption Systemic absorption; With

E. from described lyosoption system recoveries waste gas streams, wherein said waste gas streams comprises ethane, hydrogen or its combination.

5. method according to claim 4, comprises further:

6. the method described in claim 4 to 5, comprises further:

Described middle hydrocarbon stream is distilled into the effluent comprising iso-butane, and wherein said second bottom stream comprises iso-butane, and wherein said second bottom stream is substantially free of alkene.

7. the method for Component seperation in polymer production system, comprising:

A. olefinic monomer is made to be polymerized in the first polymer reactor, with m-polymerizate stream in producing;

B. in m-polymerizate stream in described being separated into m-air-flow and in m-polymer flow, in wherein said, m-air-flow comprises ethane, unreacted ethene and hydrogen; With

C. make described in m-polymer flow be polymerized in the second polymer reactor.

8. method according to claim 7, described separating step comprise reduce described in the pressure of m-polymerizate stream so that flash distillation ethene, ethane, hydrogen or its combination.

9. the method for Component seperation in polymer production system, comprising:

A. olefinic monomer is made to be polymerized in the first polymer reactor;

B. by m-polymerizate stream be separated in m-air-flow and in m-polymer flow, in wherein said, m-air-flow comprises ethane and unreacted ethene;

C. make described in m-polymer flow be polymerized in the second polymer reactor; With

D. before described second polymer reactor, scavenger is introduced.

10. method according to claim 9, described introduced before described second polymer reactor scavenger comprise described scavenger is introduced described in m-polymerizate stream.

Method described in 11. claims 9 to 10, wherein said scavenger comprises hydrogenation catalyst.

Method described in 12. claims 9 to 11, wherein said separating step comprises:

Reduce described in the pressure of m-polymerizate stream so that flash distillation ethene and ethane.

Method described in 13. claims 9 to 12, wherein said scavenger reduced the concentration of hydrogen before described second polymer reactor.

14. in polymer production system the method for Component seperation, comprising:

B. make from the hydrogen at least partially of m-polymerizate stream in described degassed, to produce the product stream that hydrogen reduces;

C. in the product stream that described hydrogen reduces being separated into m-air-flow and in m-polymer flow, in wherein said, m-air-flow comprises ethane and unreacted ethene; With

D. make described in m-polymer flow be polymerized in the second polymer reactor.

15. methods according to claim 14, described separating step comprises the pressure reducing the product stream that described hydrogen reduces, so that flash distillation ethene and ethane.

Method described in 16. claims 14 to 15, in wherein said, in m-air-flow, the amount of hydrogen accounts for and is less than about 1wt%.

Method described in 17. claims 7 to 14, comprises further:

A. make described in m-air-flow and lyosoption system contacts, wherein from the described at least partially unreacted ethene of m-air-flow in described by described lyosoption Systemic absorption; With

B. make described lyosoption system regeneration to produce the ethene reclaimed.

18. methods according to claim 17, comprise further:

From described lyosoption system recoveries waste gas streams, wherein said waste gas streams comprises ethane.

Method described in 19. claims 1 to 6 or 18, comprises further:

Process described waste gas streams in processing.

20. methods according to claim 19, wherein said treatment facility comprises cracking unit, catalytic cracking unit, washer, converter, treating apparatus, dehydrogenator, degasifier, torch or its combination.

Method described in 21. claims 1 to 6 or 17 to 20, wherein said absorbent solvent system configuration is operate to the temperature of about 110 ℉ from about 40 ℉ in scope.

Method described in 22. claims 1 to 6 or 17 to 21, wherein said absorbent solvent system comprises copper chloride, aniline and 1-METHYLPYRROLIDONE.