Method for controlling alpha-olefin condensation in absorption medium during polyolefin production

Abstract

Disclosed herein is a method comprising discharging a product stream comprising a polymer or interpolymer, a solvent, and hydrochloric acid from a reactor into an absorber; absorbing the hydrochloric acid from the product stream in the absorber; discharging the product stream, now free of substantially all hydrochloric acid, into a first heat exchanger; wherein the first heat exchanger is operable to condense the product stream free of the hydrochloric acid from the absorber; discharging condensate from the first heat exchanger to a collection drum, the collection drum operable to receive the condensate from the first heat exchanger; separating the condensate in the collection drum into a slip stream and a secondary stream; and discharging the slip stream to a compressor; wherein the compressor is operable to pressurize the slip stream prior to recycling the slip stream to the absorber.

Description

[0001] Cross-reference to related applications

[0002] This application claims the benefit of U.S. Application No. 63 / 108,638, filed November 2, 2020, the full text of which is incorporated herein by reference. Background Technology

[0003] This article discloses a method for controlling the condensation of α-olefins in an absorption medium during polyolefin production.

[0004] α-olefin comonomers (such as, for example, 1-octene, 1-hexene, 1-butene, etc.) are copolymerized with ethylene monomers in solution (or in slurry) to produce polyethylene copolymers. When Ziegler-Natta catalyst is used to catalyze the polymerization of these monomers and comonomers, hydrochloric acid is generated as a byproduct of the catalyst deactivation process. Hydrochloric acid is undesirable and is removed by a chemical reaction to form salts in an absorbent bed containing an absorbent.

[0005] During the absorption process used to remove hydrochloric acid, some gaseous monomers and comonomers may condense in the pores of the absorbent, thereby reducing its efficiency in removing hydrochloric acid from solutions or slurries. This leads to a shortened lifespan of the absorbent bed and increased maintenance downtime, which reduces productivity and increases product costs.

[0006] Therefore, it is desirable to develop systems and methods to prevent monomers and comonomers from condensing in the absorption bed. Summary of the Invention

[0007] This document discloses a system comprising: a reactor in fluid communication with an absorber; wherein the reactor receives a reaction stream comprising a monomer, a comonomer, a solvent, and a catalyst, and converts the monomer and the comonomer into a polymer or interpolymer; wherein the absorber includes an absorption bed operable to absorb hydrochloric acid from a product stream received from the reactor; a first heat exchanger located downstream of and in fluid communication with the absorber; wherein the first heat exchanger is operable to condense gaseous outputs from the absorber; a collection drum operable to receive condensate from the first heat exchanger; wherein the condensate in the collection drum is separated into a slip stream and a secondary stream; and a compressor located downstream of the collection drum and operable to pressurize the slip stream before recirculating it to the absorber.

[0008] This document also discloses a method comprising discharging a product stream comprising a polymer or interpolymer, a solvent, and hydrochloric acid from a reactor into an absorber; absorbing the hydrochloric acid from the product stream in the absorber; discharging the product stream, now free of substantially all hydrochloric acid, into a first heat exchanger; wherein the first heat exchanger is operable to condense the hydrochloric acid-free product stream from the absorber; discharging the condensate from the first heat exchanger into a collection drum operable to receive the condensate from the first heat exchanger; separating the condensate in the collection drum into a slip stream and a secondary stream; and discharging the slip stream into a compressor operable to pressurize the slip stream before recirculating it to the absorber. Attached Figure Description

[0009] The attached figure is an exemplary schematic diagram of a system for preventing monomers and comonomers from condensing in the absorbent. Detailed Implementation

[0010] The term "ethylene-based solvent polymerization" refers to a polymerization method that utilizes one or more solvents and a coordinating catalyst. The term "ethylene-based solvent polymerization" excludes radical-based, high-pressure, and gas-phase polymerization methods.

[0011] The term “polymerization reactor” refers to any reactor or combination of reactors that can be used for solvent polymerization of ethylene, including one or more circulating reactors, isothermal reactors, tubular reactors, stirred tank reactors, batch reactors, and / or any combination thereof, either in parallel or in series.

[0012] The term “coordination catalyst” refers to a catalyst used in addition polymerization, such as Ziegler-Natta catalysts, molecular catalysts (such as catalysts with restricted geometry), or combinations thereof.

[0013] The term "polymer" refers to a polymeric compound prepared by polymerizing monomers (whether the same or different types of "comonomers"). Therefore, the general term polymer encompasses the term "homopolymer," which is usually used to refer to polymers prepared from only one type of monomer, and the term "interpolymer," as defined below.

[0014] The term "interpolymer" refers to a polymer prepared by polymerizing at least two different types of monomers. The general term "interpolymer" includes copolymers (often used to refer to polymers prepared from two different monomers) and polymers prepared from more than two different types of monomers. The term "ethylene / α-olefin interpolymer" means a polymer having units derived from ethylene and units derived from α-olefin comonomers.

[0015] The term "ethylene-based polymer" refers to a polymer containing more than 50 mol% of ethylene-derived units (based on the total amount of polymerizable monomers) and optionally containing at least one comonomer.

[0016] The term "ethylene / α-olefin interpolymer" refers to an interpolymer containing more than 50 mol% of ethylene-derived units (based on the total amount of polymerizable monomers) and at least one α-olefin.

[0017] The term "polymerization byproduct" means any compound produced in a polymerization reactor other than the intended interpolymer product, including but not limited to hydrochloric acid, catalyst byproducts, acid neutralizers, acid neutralizer byproducts, water, hydrogen, ethylene, and comonomers.

[0018] This paper discloses a solution polymerization system (for manufacturing polymers or interpolymers) comprising a reactor in fluid communication with an absorber. The reactor polymerizes a feed stream of monomers and / or comonomers in solution, while the absorber receives reaction products from the reactor and removes hydrochloric acid (which is generated as a byproduct during the polymerization process). The absorber is also part of a recycling loop that generates a slipstream at higher temperatures and pressures (compared to other conventional absorbers used for hydrochloric acid removal) and this slipstream is fed back into the absorber. Using a slipstream at higher pressures and temperatures prevents the monomers and comonomers from condensing in the pores of the absorbent. This increases the lifespan of the absorber bed used in the absorber and reduces production costs.

[0019] This paper also discloses a method for producing polymers or interpolymers in solution, comprising discharging a polymer solution from a reactor to an absorber. The absorber is used to remove hydrochloric acid generated in the reactor during the reaction. A slipstream of the product generated from the absorber is fed into a heat exchanger and a compressor to increase the temperature and pressure of the slipstream. The slipstream is then recycled back to the absorber at a flow rate, temperature, and pressure that effectively prevents the condensation of gaseous monomers and comonomers in the absorbent. This extends the lifespan of the absorber while removing hydrochloric acid from the reaction stream.

[0020] The attached figure is an exemplary schematic diagram of a polymerization system 100, which includes: a reactor 102 in fluid communication with an absorber 104; a plurality of heat exchangers 106, 112; a compressor 110; a liquid collection drum 108 (hereinafter referred to as collection drum 108); and a liquid flow position valve indicator 116 (hereinafter referred to as position indicator 116). The absorber 104 is located downstream of the reactor 102.

[0021] Downstream of absorber 104 are multiple heat exchangers 106 and 112, a collection drum 108, and a compressor 110. The first heat exchanger 106 is located downstream of absorber 104 and upstream of collection drum 108. Collection drum 108 is located upstream of compressor 110 and the second heat exchanger 112. Fluid discharged through the second heat exchanger 112 is fed back to absorber 104. Therefore, absorber 104, first heat exchanger 106, collection drum 108, compressor 110, and second heat exchanger 112 are in a recirculation loop.

[0022] Reactants are fed to reactor 102 via feed stream 202. Reaction products from reactor 102 are fed to absorber 104 via feed stream 204. Absorber 104 contains an absorbent that absorbs hydrochloric acid and discharges the gaseous reaction products (now free of hydrochloric acid) to a first heat exchanger 106 (via feed stream 206), which cools these gases to form condensate. The condensate is discharged from the first heat exchanger 106 to a liquid drum 108 via feed stream 208, where it is separated into a sliding feed stream 210 and a secondary feed stream 218. The secondary feed stream 218 is discharged and ultimately recycled back to the reactor, where the monomers and / or comonomers undergo further polymerization. A rise in the liquid level in the position indicator 116 or collection drum 108 can be used to determine the effectiveness of removing condensable gases from the absorber bed in absorber 104.

[0023] The sliding stream 210 is compressed in compressor 110 and discharged via stream 212 to a second heat exchanger 112. The second heat exchanger 112 is optional, and its selectivity depends on the temperature reached by compressor 110 for heating the sliding stream 210. If compressor 110 can heat the sliding stream to the temperature required for entry into absorber 104, the second heat exchanger 112 is not needed. However, if compressor heats the sliding stream to a temperature higher than required, the second heat exchanger 112 is deployed to cool the sliding stream to the required temperature for entry into absorber. In a preferred embodiment, polymerization system 100 uses the second heat exchanger 112.

[0024] The second heat exchanger 112 cools the slip stream to the desired temperature and feeds it to the absorber 104 via stream 214. Any unused portion of the slip stream 214 is fed back into the reactor via stream 216 for further polymerization. The temperature of stream 214 exiting from the second heat exchanger 112 is generally higher than the temperature of stream 208 exiting from the first heat exchanger 106.

[0025] The collection drum 108 is in fluid communication with the position indicator 116 via an optional pump 114. Both the position indicator 116 and the collection drum 108 can be used to measure the effectiveness (e.g., efficiency) of the system 100 in removing condensable gases from the product stream in the absorber 104. The collection drum level or position indicator 116 in 108 can be used to quantify the condensed gases removed from the absorber in the solution polymerization system 100. In other words, they can be used alone or in combination to indicate the removal of condensed gases from the absorber.

[0026] The vapor stream in the liquid collection drum 108 is used to generate a slip stream. Changes in the drum level serve as a process indicator of the amount of liquid being expelled from the medium and are a measure of the liquid collection efficiency of the absorber 104. Using the collection drum 108 to measure the absorber's efficiency is optional, as the position indicator 116 can also be used to measure the efficiency of the process of extracting monomers and / or comonomers from the absorber 104. In other words, when the solution polymerization system 100 includes the position indicator 116, the collection drum 108 can be used solely for generating a slip stream, if desired. Details of the reactants and other characteristics of the method will now be provided.

[0027] Feed stream 202 transports the reactants, catalyst, and solvent to reactor 102. The reactants include olefin monomers and comonomers. Suitable olefin monomers include ethylene and α-olefins having 3 to 12 carbon atoms. Exemplary examples of such α-olefin monomers are one or more of propylene, 1-butene, 1-pentene, 1-hexene, 1-octene, and 1-decene. 1-Butene is preferred.

[0028] Based on the total weight of the feed stream 202, olefin monomers and / or comonomers are present in the feed stream 202 in an amount of 3% to 65% by weight. In a preferred embodiment, based on the total weight of the feed stream 202, olefin monomers and / or comonomers are present in the feed stream 202 in an amount of 6% to 45% by weight.

[0029] The polymerization reaction is carried out in the presence of an inert hydrocarbon solvent. Examples of inert hydrocarbon solvents include those that can be unsubstituted or C-substituted. 1-4 C with alkyl group substitution 5-12 Hydrocarbons, such as pentane, methylpentane, hexane, heptane, octane, cyclohexane, methylcyclohexane, and hydrogenated naphtha. Examples of suitable solvents are… E" (C is commercially available from Exxon Chemical Co.) 8-12 (Aliphatic solvents)

[0030] Based on the total weight of the feed stream 202, the solvent is present in the feed stream 202 in an amount of 52% to 82% by weight. In a preferred embodiment, based on the total weight of the feed stream 202, the solvent is present in the feed stream 202 in an amount of 68% to 74% by weight.

[0031] The catalyst used may be a Ziegler-Natta catalyst, a bismetallocene catalyst, a catalyst with a defined geometry, a polyvalent aryloxy ether complex, a phosphonium imine, or a combination thereof. A Ziegler-Natta catalyst is preferred.

[0032] Based on the total weight of the feed stream 202, the catalyst is present in the feed stream 202 in an amount of 0.2 ppm to 2.4 ppm. In a preferred embodiment, based on the total weight of the feed stream 202, the catalyst is present in the feed stream 202 in an amount of 0.25 ppm to 0.40 ppm.

[0033] Monomers and / or comonomers are mixed with hydrogen and dissolved / dispersed in a solvent, then fed to reactor 102 via feed stream 202. Prior to mixing, the solvent and monomers (sometimes referred to as "feedstock") are typically purified to remove potential catalyst poisons, such as water, oxygen, or other polar impurities. Feedstock purification may employ molecular sieves, alumina beds, or oxygen-removing catalysts. The solvent may also be purified in a similar manner. The feedstock to reactor system 102 is typically cooled to below 40°C, preferably below 20°C. Cooling may occur within the reactor system or before entering the reactor. In a preferred embodiment, cooling of the feedstock may occur before entering the reactor.

[0034] Typically, the catalyst components can be premixed in the solvent used for the reaction or fed as a separate feed stream into one or more reactors in reactor 102. Reactor 102 can be a continuous stirred tank reactor (CSTR), a circulating reactor (e.g., a single-circulation reactor, a double-circulation reactor), a fluidized bed reactor, and can be a single-stage or multi-stage reactor. In one embodiment, this method can employ multiple catalysts in one or more reactors.

[0035] In one embodiment, reactor 102 operates at a temperature greater than 40 kgf / cm². 2 Preferably greater than 45 kgf / cm³ 2 And more preferably greater than 50 kgf / cm 2 The reactor operates under pressure. In one embodiment, the reactor 102 operates at a temperature ranging from 155°C to 210°C. In one embodiment, the temperature of the polymer solution exiting the reactor 102 via the feed stream 204 can be from 165°C to 215°C, preferably from 185°C to 205°C.

[0036] This method can be used to prepare olefin-based polymers, such as ethylene homopolymers and interpolymers, interpolymers with other olefins (e.g., copolymers or terpolymers), and optionally interpolymers with dienes (e.g., EPDM terpolymers).

[0037] In one embodiment, based on the content of the product stream 204 between reactor 102 and absorber 104, the product stream 204 leaving the reactor contains 0.75 wt% to 5.5 wt% ethylene, up to 65 wt% α-olefin, up to 75 wt% hydrocarbon solvent, and up to 80 parts per million (ppm) of hydrochloric acid.

[0038] In a preferred embodiment, based on the content of the product stream 204 between reactor 102 and absorber 104, the product stream 204 leaving reactor 102 contains 0.75% by weight (wt%) to 5.50 wt% of ethylene in monomeric form, up to 15 wt% of 1-butene, up to 75 wt% of hydrocarbon solvent, and 10 parts per million (ppm) to 30 ppm of hydrochloric acid.

[0039] The product stream 204 is discharged into an absorber 104 containing an absorbent bed (not shown). The absorbent comprises materials with a surface area (measured using the BET nitrogen porosity method) of 150 m² / g (m³). 2 / g) to 2000m 2 / g, preferably 200m 2 / g to 1000m 2 A porous material of / g is used to effectively absorb hydrochloric acid gas generated as a byproduct during the polymerization reaction. The hydrochloric acid gas reacts in the pores of the absorbent to form salts. When the absorbent becomes saturated with the absorbent, the absorbent bed can be replaced with a new bed. The bulk density of the absorbent is 752 kg / m³. 3 Up to 753 kg / m 3 The dynamic chloride capacity of this absorbent is 12 wt% to 15 wt%.

[0040] Suitable examples of absorbents are alumina, silica, clay (e.g., kaolin), exfoliated clay (e.g., vermiculite), calcium sulfate, etc., or combinations thereof. A preferred absorbent is alumina.

[0041] It is undesirable for the absorbent to absorb other monomers or comonomers that can be used to produce the polymer. It is desirable to recycle these monomers and comonomers back to the reactor, where they can be consumed in polymer production. However, in other conventional solution-based methods for producing polyolefins, gaseous comonomers (such as, for example, 1-butene, 1-octene, 1-hexene, etc.) can also condense in the pores of the absorbent, in addition to gaseous hydrochloric acid. To prevent the condensation of monomers and comonomers in the pores of the absorbent, a portion of the feed stream 206 discharged from absorber 104 is recycled back to absorber 104 at a higher temperature and pressure than the original product feed stream 204 discharged from reactor 102. This portion of the original feed stream recycled back to absorber 104 is referred to as the slip stream. The use of a sliding stream with higher pressure and temperature than the original product stream 204 prevents monomers and / or comonomers present in the combined stream 205 (which includes stream 204 and recirculated stream 214 (described later)) from condensing in the pores of the absorbent.

[0042] The feed stream 206 discharged from absorber 104 contains a reduced amount of hydrochloric acid (compared to the product feed stream 204) and is discharged into first heat exchanger 106. In one embodiment, based on the content of the feed stream 206 between absorber 104 and first heat exchanger 106, the feed stream 206 leaving absorber 104 contains 60 wt% to 100 wt% ethylene, up to 40 wt% α-olefin, up to 10 wt% hydrocarbon solvent, and up to 1 ppm hydrochloric acid.

[0043] In a preferred embodiment, based on the content of the feed stream 206 between absorber 104 and first heat exchanger 106, the feed stream 206 exiting absorber 104 contains 70 wt% to 100 wt% ethylene, up to 40 wt% 1-butene, up to 10 wt% hydrocarbon solvent, and 0 ppm to 1 ppm hydrochloric acid. In one embodiment, the feed stream 206 is free of hydrochloric acid after exiting absorber 104.

[0044] The first heat exchanger 106 preferably cools the feed stream 206 (thus condensing the gas into a liquid) and discharges the feed stream into a liquid collection drum 108. The condensation of the gas into a liquid in the collection drum 108 reduces the volume of material discharged from the drum 108 to the compressor 110. This reduces the compressor load.

[0045] Heat exchanger 106 is at least one of a shell-and-tube heat exchanger, a plate heat exchanger, a plate-fin heat exchanger, or a plate-and-shell heat exchanger. In a preferred embodiment, heat exchanger 106 is a shell-and-tube heat exchanger that uses cooled ethylene glycol to condense the gas released from absorber 104 into a liquid.

[0046] As described above, the condensate stream 208 discharged from the first heat exchanger 106 is discharged into a liquid collection drum 108. The height (or volume) of the liquid column in the liquid collection drum 108 can be used to measure the efficiency of gas removal from the absorber 104 during this process. The collection drum operates at a temperature of -20°C to +20°C, preferably -10°C to +10°C. These temperatures are favorable for the condensation of any gases that may not have yet undergone condensation in the first heat exchanger 106.

[0047] The amount of liquid collected per unit time in the liquid collection drum 108 provides information about the performance of the absorber 104. If a significant amount of monomers and / or comonomers condense in the pores of the absorbent, the amount of liquid collected in the liquid collection drum 108 will be less than the amount collected if the monomers and / or comonomers do not substantially condense in the pores of the absorbent. In other words, the collection drum 108 can be used to determine the effectiveness of selected pressures, temperatures, and flow rates of the sliding feed flow 210. These will be discussed in detail below.

[0048] As shown in the figure, a portion of the condensate in collection drum 108 is discharged back into the absorber as a sliding feed stream 214, while the remainder is discharged and eventually recirculated back into the reactor via position indicator 116 and optional pump 114. Position indicator 116 can be a mass flow meter or a liquid flow valve position indicator, where the valve's position indicates the flow rate. A larger flow rate indicated by position indicator 116 will mean that a substantially smaller amount of monomer and / or comonomer condensation occurs in the pores of the absorbent compared to a lower flow rate.

[0049] The sliding material flow 210 constitutes 70 wt% to 80 wt% of the material flow 208 entering the collection drum 108. The sliding material flow 210 is discharged into the compressor 110, where it is compressed to 15 kg / cm². 2 Up to 20 kg / cm 2 Preferably 17 kg / cm 2 Up to 18kg / cm 2 The pressure. During compression, the temperature of the sliding material flow 212 can be from 90°C to 250°C, preferably from 110°C to 120°C. The compressor 110 heats the sliding material flow 210 during compression.

[0050] If the sliding material stream heats up to a temperature 20°C to 250°C, preferably 20°C to 40°C, higher than the temperature of the product stream 204 at the absorber inlet during compression, then the second heat exchanger 112 is an optional feature. On the other hand, if compression results in a temperature rise higher than the desired temperature at the absorber inlet, the second heat exchanger 112 can be used to reduce the temperature to the desired value, which is 20°C to 250°C, preferably 20°C to 40°C, higher than the temperature of the product stream 204.

[0051] The pressurized sliding stream 212 is discharged from the compressor 110 to the second heat exchanger 112, where its temperature is reduced to a value 20°C to 250°C higher than the temperature of the product stream 204. Therefore, the second heat exchanger 112 serves to reduce the temperature of the pressurized sliding stream 212. In a preferred embodiment, the pressure of the recirculated sliding stream 214 discharged from the second heat exchanger 112 is 15 kg / cm³. 2 Up to 20kg / cm 2 Preferably 17 kg / cm 2 Up to 18kg / cm 2 The temperature of the recirculated sliding feed stream 214 is preferably 20°C to 40°C higher than the temperature of the product feed stream 204 entering the absorber 104 from the reactor 102.

[0052] The increased pressure relative to the product stream 204, and the increased pressure of the recirculated sliding stream 214, promotes an increase in the flow rate of the combined stream 205 entering the absorber 204. Stream 205 is a combination of the product stream 204 discharged from reactor 102 and the sliding stream 214 discharged from the second heat exchanger 112. Stream 205 is referred to as the combined stream. This increased flow rate of the combined stream 205, along with the increased temperature of the gas entering the absorber 104 (due to the increased temperature, increased pressure, and increased flow rate of the recirculated sliding stream 214), prevents the condensation of gaseous monomers and comonomers in the absorbent (contained in the absorber bed). As can be seen from the figure, the non-recirculated portion of the sliding stream 214 is discharged and eventually recirculated back into the reactor for further treatment. This portion of the sliding stream 214 is designated as stream 216.

[0053] Based on the total weight of the recirculated flow 214, the recirculated sliding flow 214 contains 55 wt% to 100 wt% ethylene, up to 40 wt% α-olefin, up to 1 wt% hydrocarbon solvent, and up to 1 ppm hydrochloric acid.

[0054] In a preferred embodiment, based on the total weight of the recycled stream 214, the recycled stream 214 contains 55 wt% to 100 wt% ethylene, up to 40 wt% 1-butene, up to 1 wt% hydrocarbon solvent, and 0 ppm to 1 ppm hydrochloric acid.

[0055] Increased temperature and pressure do not adversely affect the absorption of gaseous hydrochloric acid (compared to conventional systems without increased temperature and pressure), and the chemical reactions of gaseous hydrochloric acid occurring in the pores of the absorbent remain the same or are improved compared to the absorbents used in conventional systems. Because gaseous monomers and / or comonomers do not condense in the absorbent in the disclosed system, the usable service life (i.e., life cycle) of the absorption bed is extended compared to conventional absorption beds (used in conventional absorption methods) without increased temperature, increased pressure, and increased flow rate.

[0056] In one embodiment, the usable service life is extended by at least 10%, preferably at least 25%, and more preferably at least 40%, compared to a conventional absorption bed deployed in a conventional absorption method. A conventional absorption method is an absorption method in which there is no sliding feed flow recirculated back to the absorber. In a conventional absorption method, the feed temperature to the absorber is at least 20°C lower than the feed temperature in the disclosed method, which includes a sliding feed flow. Preferably, it is at least 30°C lower, and more preferably at least 35°C lower.

[0057] Although the invention has been described with reference to some embodiments, those skilled in the art will understand that various changes can be made and elements can be substituted with equivalents without departing from the scope of the invention. Furthermore, many modifications can be made to adapt particular situations or materials to the teachings of the invention without departing from the essential scope of the invention. Therefore, it is intended that the invention be limited to the specific embodiments disclosed as the best mode contemplated for carrying out the invention, but that the invention encompass all embodiments falling within the scope of the appended claims.

Claims

1. A system comprising: A reactor, in fluid communication with an absorber; wherein the reactor receives a reaction stream comprising olefin monomers, comonomers, solvents and catalysts, and converts the olefin monomers and comonomers into olefin-based polymers or interpolymers; wherein the absorber includes an absorption bed operable to absorb hydrochloric acid from the product stream received from the reactor. A first heat exchanger is located downstream of and in fluid communication with the absorber; wherein the first heat exchanger is operable to condense the gaseous output from the absorber. A collection drum operable to receive condensate from the first heat exchanger; The condensate in the collection drum is separated into a sliding stream and a secondary stream; as well as compressor; The compressor is located downstream of the collection drum, and the compressor is operable to pressurize and heat the slip stream before recirculating it to the absorber to obtain a higher pressure and temperature than the product stream.

2. The system of claim 1, wherein the compressor heats the sliding feed stream to a temperature at least 20 degrees higher than the temperature of the product feed stream received at the inlet of the absorber.

3. The system of claim 1, further comprising a second heat exchanger located downstream of the compressor and upstream of the absorber; wherein the second heat exchanger is operable to reduce the temperature of the pressurized sliding feed received from the compressor.

4. The system of claim 1, further comprising a position indicator located downstream of the collection drum; wherein the position indicator is operable to determine the condensation efficiency of olefin monomers and / or comonomers in the absorber; and wherein the condensation efficiency is determined by the flow rate of the condensate or by the valve position.

5. The system of claim 1, wherein the collection drum is operable to indicate the condensation efficiency of the absorber in preventing the condensation of the olefin monomers and / or the comonomers used to produce the olefin-based polymer or the interpolymer; and wherein the efficiency is determined by the height of the column of condensate in the collection drum.

6. The system of claim 2, wherein the temperature is at least 20 to 40 degrees higher than the temperature of the product stream received at the absorber.

7. The system of claim 1, wherein the system is operable to remove substantially all hydrochloric acid from the product stream while preventing the olefin monomers and / or the comonomers from the product stream from condensing in the absorbent bed.

8. A method, the method comprising: The product stream, which contains olefin-based polymers or interpolymers, solvents, and hydrochloric acid, is discharged from the reactor into the absorber. The hydrochloric acid is absorbed from the product stream in the absorber; The product stream, now free of substantially all hydrochloric acid, is discharged into the first heat exchanger; The first heat exchanger is operable to condense the hydrochloric acid-free product stream from the absorber; Condensate is discharged from the first heat exchanger to a collection drum, which is operable to receive the condensate from the first heat exchanger; The condensate in the collection drum is separated into a sliding flow and a secondary flow; as well as The sliding material flow is discharged into the compressor; The compressor is operable to pressurize and heat the slip stream before recirculating it to the absorber to obtain a higher pressure and temperature than the product stream.

9. The method of claim 8, wherein the compressor heats the sliding feed stream to a temperature at least 20 degrees higher than the temperature of the product feed stream received at the inlet of the absorber.

10. The method of claim 8, further comprising discharging the pressurized sliding stream from the compressor to a second heat exchanger; wherein the second heat exchanger is located downstream of the compressor and upstream of the absorber; wherein the second heat exchanger is operable to reduce the temperature of the pressurized sliding stream received from the compressor to a temperature at least 20 degrees higher than the temperature of the product stream received at the inlet of the absorber.

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