Energy recovery method

Abstract

The present invention is a method for energy recovery comprising the steps of: a) providing a hot fluid stream; and b) thermally contacting the hot fluid stream with an aqueous condensate in a heat exchanger, thereby transferring heat from the hot fluid stream to the aqueous condensate and vaporizing at least a portion of the aqueous condensate to a temperature T 1 and pressure p 1 and c) subjecting the water vapor stream to at least one compression step to a pressure p 2 and d) using the compressed water vapor stream for energy recovery, thereby obtaining a stream comprising an aqueous condensate, 1 Pressure on p 2 The ratio of p 2 / p 1 , is 5 to 50; and an energy recovery facility, 1 and pressure p 1 A water vapor stream having a pressure p 2 and one or more means for compressing the water vapor stream, connected in series, at a temperature T 1 and pressure p 1 The steam stream having a pressure p 2 and the use in said method or installation for obtaining a compressed water vapor stream having

Description

Technical Field

[0001] The present invention relates to an energy recovery method in which thermal energy is transferred from a high-temperature fluid stream to an aqueous condensate in a heat exchange process, thereby obtaining a water vapor stream, which is then subjected to at least one heating and compression step, from which a heated and compressed water vapor stream is obtained for energy recovery.

Background Art

[0002] In connection with efforts to reduce carbon dioxide emissions, one task is to reduce the consumption of carbonaceous primary energy. This has also focused on the recovery of energy in the form of heated or compressed fluids, which can be used, for example, as an energy source in industrial processes.

[0003] Industrial processes, such as chemical manufacturing processes, for example, processes for polymerizing polymers, often consume a great deal of thermal energy or electrical energy to heat or boil, for example, to the temperatures and pressures required for the use or reuse of streams, or to supply energy to the manufacturing facilities of the chemical manufacturing process. On the other hand, a large amount of waste heat is generated, for example, by cooling a product stream. However, most of these cooling streams have temperatures that are too low to be directly reused as a heating medium or for the generation of electrical energy. As an example, well-established licensed multi-stage polymerization processes for polymerizing polyolefins are, among others, for example, Borstar® from Borealis AG or Spheripol™ from LyondellBasell. In these processes, two or more polymerization stages are connected in series, followed by a downstream process for treating the polymerized polyolefin. In each of the polymerization stages and the downstream process, waste heat from the cooling of the product stream is obtained, but this is currently mostly wasted.

[0004] International Publication No. WO 2009 / 010514 A1 pamphlet and International Publication No. WO 2011 / 000925 A1 pamphlet disclose a method for recovering heat from a cooling fluid used to cool a polymerization reaction in a loop reactor by transferring thermal energy from the cooling fluid to a working fluid in one heat exchange step, wherein the working fluid is phase-converted, thereby returning energy in the form of heat and / or electricity and / or heat output to the polymerization process. However, these methods are only applicable to the polymerization process in a loop reactor, require several intermediate streams for transferring thermal energy, and this transfer inevitably results in energy losses and reduced efficiency.

Prior Art Documents

Patent Documents

[0005]

Patent Document 1

Patent Document 2

Summary of the Invention

Problems to be Solved by the Invention

[0006] Accordingly, there is a need for a highly efficient method of recovering energy that can be applied to all types of waste heat generated not only in industrial processes but also in other situations where waste heat is generated, such as power generation, engines, electronic devices, or housings, to name a few.

[0007] Surprisingly, when heat is transferred from a high-temperature fluid stream from any heat source to an aqueous condensate to obtain a water vapor stream, this water vapor stream can be efficiently fed to one or more heating and compression steps for generating a heated and compressed water vapor stream having a temperature and pressure suitable for direct use, preferably as a heating medium, in energy recovery.

Means for Solving the Problem

[0008] The present invention relates to an energy recovery method, a) supplying a high-temperature fluid stream; b) thermally contacting the high-temperature fluid stream with an aqueous condensate in a heat exchanger to transfer heat from the high-temperature fluid stream to the aqueous condensate and vaporize at least a portion of the aqueous condensate to obtain a water vapor stream having a temperature T 1 and a pressure p 1 ; c) subjecting the water vapor stream to at least one compression step to obtain a compressed water vapor stream having a pressure p 2 ; d) using the compressed water vapor stream for energy recovery to obtain a stream containing an aqueous condensate and · the ratio of the pressure p 1 to the pressure p 2 , p 2 / p 1 , is 5 to 50 relates to a method.

[0009] Furthermore, the present invention relates to a facility for energy recovery, · Transfer heat from a high-temperature fluid stream to an aqueous condensate to obtain a water vapor stream having a temperature T 1 and a pressure p 1 and a heat exchanger for obtaining a water vapor stream having a temperature T · One or more, preferably 1 to 5, more preferably 2 to 4, and most preferably 2 or 3, connected in series, having a temperature T 1 and a pressure p 1 Compress the water vapor stream having a temperature T 2 and a pressure p 2 To obtain a compressed water vapor stream having a temperature T · Pressure p 2 Use the compressed water vapor stream having a temperature T To obtain a stream containing an aqueous condensate, and means for this purpose · Optionally, the compressed water vapor stream is transported from one upstream means for compressing the water vapor stream to the next downstream means for compressing the water vapor stream in a series of means for compressing the water vapor stream · Pressure p 2 The compressed water vapor stream having a temperature T 2 Transport the compressed water vapor stream having a temperature T To the means for using the compressed water vapor stream having a temperature T

[0010] Furthermore, the present invention relates to means for compressing one or more, preferably 1 to 5, more preferably 2 to 4, and most preferably 2 or 3, steam streams connected in series, preferably at least one, for example 1 or 2, preferably 1 heat pump compressor, each heat pump compressor comprising one or more, preferably 1 to 5, more preferably 2 to 4, and most preferably 2 or 3 compression stages connected in series, for use in the above or both of the following methods or manufacturing facilities for compressing a steam stream having a temperature T 1 and a pressure p 1 to obtain a compressed steam stream having a pressure p for direct energy recovery 2 in order to obtain a compressed steam stream having a pressure p for direct energy recovery

[0011] "Direct use" or "direct energy recovery" in the sense of the present invention means that the compressed steam stream is used as an energy source such as a heating source. Thereby, the compressed steam stream can be applied as an energy source without further manipulating the temperature and / or pressure of the compressed steam stream

Brief Description of the Drawings

[0012]

Figure 1

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[0013] Method In a first aspect, the present invention is an energy recovery method comprising: a) supplying a high-temperature fluid stream; b) thermally contacting the high-temperature fluid stream with an aqueous condensate in a heat exchanger, thereby transferring heat from the high-temperature fluid stream to the aqueous condensate and vaporizing at least a portion of the aqueous condensate to obtain a water vapor stream having a temperature T 1 and a pressure p 1 ; c) subjecting the water vapor stream to at least one compression step to obtain a compressed water vapor stream having a pressure p 2 ; d) using the compressed water vapor stream for energy recovery, thereby obtaining a stream containing an aqueous condensate ; · the ratio of the pressure p 1 to the pressure p 2 , p 2 / p 1 , is from 5 to 50 relates to a method.

[0014] The high-temperature fluid stream preferably has a temperature T of 20 to 150 °C, more preferably 25 to 130 °C, and most preferably 30 to 110 °C. f It has. Therefore, the method of the present invention can also be used to recover energy from a fluid stream having a moderate temperature. Therefore, in this context, the term "high temperature" means that heat can be exchanged from the high-temperature fluid stream to the first heat transfer fluid so that the temperature T of the high-temperature fluid stream f is higher than the temperature T of the first heat transfer fluid before entering the first heat exchanger 0 It only means that.

[0015] The high-temperature fluid stream can be provided from any type of fluid stream at a high temperature. The source of the high-temperature fluid stream can be an industrial process, or any other situation where waste heat is generated in the form of a high-temperature fluid stream, such as power generation, engines, electronic devices or housings.

[0016] In one preferred embodiment, the high-temperature fluid stream is provided from an industrial process, more preferably from a chemical manufacturing process. The chemical manufacturing process can be any process for manufacturing chemical products, and can be a process from which heat can be recovered from the high-temperature fluid stream. In one specific embodiment, the chemical manufacturing process is a polymerization process. The polymerization process is preferably a process for polymerizing an α-olefin polymer. The polymerization process is preferably a low-pressure process for polymerizing an α-olefin polymer in the presence of a polymerization catalyst.

[0017] The polymerization catalyst can be any suitable catalyst for polymerizing an α-olefin polymer, such as a supported or unsupported Ziegler-Natta catalyst or a metallocene catalyst.

[0018] The α-olefin polymer can be a homopolymer or copolymer of ethylene and / or an α-olefin monomer having 3 to 12 carbon atoms, such as ethylene, propylene, 1-butene, 1-hexene or 1-octene. Preferred are ethylene homopolymers, or copolymers of ethylene and one or more comonomers selected from α-olefin comonomers having 3 to 12 carbon atoms, such as propylene, 1-butene, 1-hexene and / or 1-octene, and propylene homopolymers, or copolymers of propylene and one or more comonomers selected from ethylene or α-olefin comonomers having 4 to 12 carbon atoms, such as ethylene, 1-butene, 1-hexene and / or 1-octene.

[0019] The polymerization process may be a one-step polymerization process or a multi-step polymerization process. In a one-step polymerization process, the polymer polymerization is carried out in one polymerization reactor that can be selected from a slurry-phase reactor, such as a loop reactor, and a gas-phase reactor, such as a fluidized-bed gas-phase reactor. The polymerization process is preferably a multi-step polymerization process in which two or more reactors, preferably 2 to 6 reactors, such as 2, 3, 4, 5 or 6 reactors, are connected in series. These two or more reactors are usually selected from a slurry-phase reactor, such as a loop reactor, and a gas-phase reactor, such as a fluidized-bed gas-phase reactor. Downstream of the reactor stage(s) of the polymerization process, the polymer is further processed. In this downstream processing stage, the polymer is preferably separated from unreacted monomers and other components of the production stream. Further, the polymer is preferably compounded in an extruder with applicable additives as known in the art.

[0020] Typical multi-step polymerization processes to which the method of the present invention is applicable include, inter alia, for example, Borstar® PE and Borstar® PP from Borealis AG or Spheripol™ from LyondellBasell.

[0021] The high-temperature fluid stream can be provided from any process stage of a chemical manufacturing process, for example, one or more or all of the manufacturing stages in which a chemical product or any precursor or intermediate is manufactured, and / or a processing stage downstream from the manufacturing stage(s), such as a purification stage or a compounding stage.

[0022] It is particularly preferred that the high-temperature fluid stream is not a cooling stream from a heat exchange process. Instead, the high-temperature fluid stream is preferably a stream obtained directly without indirect heat exchange or energy transfer.

[0023] The high-temperature fluid stream may be a slurry stream, a liquid stream or a gaseous stream. When it is a slurry stream or a liquid stream, the high-temperature fluid stream preferably has a temperature T in the range of 20 to 120 °C, more preferably 25 to 110 °C, and most preferably 30 to 100 °C. f to have. When it is a gaseous stream, the high-temperature fluid stream preferably has a temperature T in the range of 50 to 150 °C, preferably 55 to 130 °C, and most preferably 65 to 110 °C. f and a pressure in the range of 5 to 50 bar (bara), preferably 8 to 40 bar, and most preferably 10 to 35 bar.

[0024] In an embodiment of the chemical manufacturing process, the high-temperature fluid stream is preferably a high-temperature product stream. In an embodiment of the above polymerization process, the high-temperature product stream is preferably selected from a high-temperature polymer slurry stream in a slurry-phase polymerization stage, a high-temperature recycle gas stream from a gas-phase polymerization stage, or a high-temperature polymer stream from a processing stage downstream from the polymerization stage(s), such as an extrusion stage. The high-temperature fluid stream can also be the primary water circuit of an extruder in a processing stage downstream from the polymerization stage, such as an extrusion stage.

[0025] The high-temperature fluid stream provided from the polymerization process preferably contains monomers, optionally comonomers (both defined above), and optionally a chain transfer agent such as hydrogen. When it is a high-temperature polymer slurry stream in the slurry-phase polymerization stage or a high-temperature polymer stream from a downstream processing stage from the polymerization stage(s), the high-temperature fluid stream preferably contains a polymer.

[0026] The high-temperature fluid stream is preferably transported directly to the heat exchange process. In this regard, "directly" means that the high-temperature fluid stream does not undergo any further treatment that would manipulate the temperature of the high-temperature fluid stream.

[0027] In the heat exchanger, the high-temperature fluid stream is brought into thermal contact with an aqueous condensate. Thereby, heat is transferred from the high-temperature fluid stream to the aqueous condensate, and a heated aqueous condensate and a fluid stream having a temperature T f1 are obtained.

[0028] T f1 is lower than the temperature T f of the high-temperature fluid stream. T f1 is preferably in the range of 15 to 145 °C, more preferably 20 to 125 °C, and even more preferably 25 to 98 °C.

[0029] The aqueous condensate is preferably liquid water such as make-up water. The aqueous condensate is preferably used only when the aqueous condensate is used as a heating and cooling medium and in a closed energy recovery cycle used to generate electrical energy. The aqueous condensate is preferably not separated from the product stream of the industrial production process or introduced into the product stream of the industrial production process.

[0030] When introduced into the heat exchanger, the aqueous condensate is preferably at least partially liquid, for example at least 60% by weight is liquid, preferably at least 75% by weight is liquid, and most preferably at least 90% by weight is liquid. Thereby, the non-liquid part of the aqueous condensate is gaseous up to 40% by weight, preferably up to 25% by weight, and most preferably up to 10% by weight. In a preferred embodiment, the aqueous condensate is 100% liquid depending on the temperature and pressure conditions when introduced into the heat exchanger.

[0031] When introduced into the heat exchanger, the aqueous condensate preferably has a temperature T of 40°C to 99°C, preferably 50°C to 98°C, and most preferably 55°C to 95°C. c and / or a pressure p of 1 to 10 bar (a), preferably 2 to 9 bar (a), and most preferably 3 to 8 bar (a). c It has.

[0032] During heat transfer, the heated aqueous condensate is preferably at least partially vaporized so that a steam stream having a temperature T 1 and a pressure p 1 is obtained. In some embodiments, the heated aqueous condensate is completely vaporized. If the heated aqueous condensate is only partially vaporized, the remaining aqueous condensate may be separated from the steam stream and recycled to the heat exchanger as aqueous condensate. The aqueous condensate can also be removed from the bottom of the heat exchanger to remove undesirable components such as salts, heavier components, rust, or other dirt from the heat exchanger.

[0033] The steam stream preferably has a temperature T in the range of 30°C to 150°C, preferably 40°C to 135°C, and most preferably 50°C to 100°C. 1 and / or a pressure p in the range of 0.04 bar (a) to 4.76 bar (a), preferably 0.07 to 3.13 bar (a), and most preferably 0.12 to 1.01 bar (a). 1 It has. For direct use as a heat source, or for generating electrical energy, the temperature T of the steam stream 1 and the pressure p 1 are usually too low for efficient energy recovery to be possible. Therefore, in the method of the present invention, the pressure of the steam stream is increased to the pressure p 2 until it reaches.

[0034] To increase the pressure of the steam stream, the steam stream is subjected to at least one, for example 1 to 5, preferably 2 to 4, most preferably 2 or 3 compression steps to obtain a heated and compressed steam stream having a temperature T 2 and a pressure p 2 For the compression step(s), preferably at least one, for example 1 or 2, preferably 1 heat pump compressor is used. Each heat pump compressor preferably includes at least one, preferably 1 to 5, more preferably 2 to 4, most preferably 2 to 3 compression stages connected in series. At least one heat pump compressor is preferably part of a heat pump as known in the art.

[0035] When multiple compression steps are used, the compression steps are preferably arranged continuously by using one or more heat pump compressors, and at least one, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 compression stages are arranged continuously.

[0036] When multiple compression steps are used, the compression steps are preferably arranged continuously by using one or more heat pump compressors, and at least one, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 compression stages are arranged continuously. In a continuous configuration, the water vapor stream is first subjected to a first compression step, preferably in the first (initial) upstream compression stage of a heat pump compressor, whereby the pressure of the water vapor stream is increased by a first increment in the first step. The water vapor stream compressed in the first step is then preferably subjected to the next downstream compression step in the second compression stage of the heat pump compressor located downstream from the first upstream compression stage of the heat pump exchanger, whereby the pressure of the water vapor stream is increased by a second increment in the second step. This is optionally repeated until a compressed first heat transfer fluid having a pressure p 2 is obtained.

[0037] Between at least one, for example 1 to 5, preferably 2 to 4, most preferably 2 to 3 compression steps as described above, the temperature of the water vapor stream rises to temperature T 2 . When multiple compression steps are used, the temperature of the water vapor stream typically increases in increments during each compression step in parallel with the increments of pressure increase as discussed above.

[0038] Between at least one, for example 1 to 5, preferably 2 to 4, most preferably 2 or 3 compression steps as described above, the temperature of the water vapor stream preferably rises to temperature T 2 . When multiple compression steps are used, the temperature of the water vapor stream typically increases in increments during each compression step in parallel with the increments of pressure increase as discussed above.

[0039] The increments of temperature and pressure increase in subsequent compression steps typically depend on the volumetric stream of the water vapor stream and the dimensions and output of each heat pump compressor. The increment of pressure increase determined as the ratio of p out / p in in each compression step is preferably independently in the range of 1.3 to 3, preferably 1.5 to 2.5. Preferably, the increment of the temperature rise in each compression step is independently in the range of 25 to 250 K, preferably 50 to 200 K.

[0040] In some embodiments, the temperature rise in the compression step can result in a temperature of the compressed water vapor stream of about 300 °C. Temperatures above 300 °C are undesirable due to the vulnerability or likelihood of failure of the materials of the pipes, armature, and mounting parts affected. Therefore, it is preferable that the temperature of the compressed water vapor stream after one or more compression steps, preferably after each compression step, is reduced so that the temperature of the compressed water vapor stream does not exceed 300 °C.

[0041] The temperature of the compressed water vapor stream can be reduced after one or more heating and compression steps, preferably after each heating and compression step, by combining the compressed water vapor stream with a higher-pressure aqueous condensate and a portion of the aqueous condensate of step d). The compressed water vapor stream is preferably combined with a higher-pressure aqueous condensate in a superheat reducer.

[0042] The amount of compression steps is preferably proposed by considering the expected pressure increase increment of each compression step to obtain a compressed water vapor stream having a pressure p 2 The compressed water vapor stream having a pressure p

[0043] The compressed water vapor stream having a pressure p 2 preferably has a temperature T 2 The compressed water vapor stream having a pressure p Preferably, the temperature T 2 is in the range of 125 °C to 300 °C, preferably 135 °C to 275 °C, most preferably 140 °C to 250 °C, and / or the pressure p 2 is in the range of 3 bar(a) to 12 bar(a), preferably 4 to 10 bar(a), most preferably 5 to 8 bar(a).

[0044] The temperature T 2 is the temperature T1 is preferably 50K to 250K, more preferably 65K to 150K, and most preferably 75K to 125K higher.

[0045] The pressure p 1 for the pressure p 2 ratio of, p 2 / p 1 is 5 to 50, preferably 10 to 40, and most preferably 15 to 30.

[0046] The pressure p 2 of the compressed steam stream is used for energy recovery.

[0047] One suitable means of energy recovery is to use the compressed steam stream as a heating medium. In a manufacturing facility, the steam stream can be used as a heating medium to heat, for example, a product stream, any other stream, or a component of the manufacturing site, either at any stage of the chemical manufacturing process or even in the heating system of the manufacturing facility. Preferably in a polymerization process as discussed above, the compressed steam stream can be used, for example, to replace the steam in a reboiler in a process for recovering monomers, comonomers, and other reactants of the polymerization process, or to heat a flash tank in a gas-phase polymerization stage. A method suitable for thermal energy storage is, for example, a method using a reverse condensation reaction such as a chemical heat pump, which has been commercialized by Qpinch and is described, for example, in particular in WO 2014 / 016405 A1 pamphlet. A suitable method for generating electricity has been commercialized by Climeon and is described, for example, in particular in EP 2689111 A1 specification. For example, an excess compressed steam stream not used for energy recovery within an industrial process can also be used as a heating medium outside the industrial process or for other forms of energy recovery.

[0048] Pressure p 2 By using a compressed water vapor stream having a pressure p for energy recovery, the temperature and pressure of the compressed water vapor stream are reduced to such an extent that the water vapor stream is at least partially condensed and a stream containing an aqueous condensate is obtained.

[0049] After being used for energy recovery, the stream containing the aqueous condensate is preferably at least partially liquid, for example, at least 60% by weight is liquid, preferably at least 75% by weight is liquid, and most preferably at least 90% by weight is liquid. Thereby, the non-liquid portion of the aqueous condensate is gaseous up to 40% by weight, preferably up to 25% by weight, and most preferably up to 10% by weight. In some embodiments, the aqueous condensate is 100% by weight liquid depending on the temperature and pressure conditions after energy recovery.

[0050] Preferably, a stream containing the aqueous condensate obtained from the compressed water vapor stream used for heat recovery is subjected to a vapor separation step to obtain a second water vapor stream and an aqueous condensate. The aqueous condensate can be used in a heat exchanger to transfer heat from a high-temperature fluid stream to the aqueous condensate and vaporize at least a part of the aqueous condensate to obtain a water vapor stream having a temperature T 1 and a pressure p 1 The second water vapor stream can preferably be combined with the compressed water vapor stream after the first compression step. From the following proposed examples, when the second water vapor stream is combined with the compressed water vapor stream, the temperature T 2 and the pressure p 2 ​To obtain a compressed water vapor stream, it can be seen that the energy consumption in the compression process, usually in the form of power consumption of a heat pump compressor, requires only a lower amount. As a result, when the second water vapor stream is combined with the compressed water vapor stream, the COP (Coefficient of Performance) of the heat pump as the consumed electricity to the generated stream is higher.

[0051] Manufacturing equipment In a further aspect, the present invention is an installation for energy recovery, transferring heat from a high-temperature fluid stream to an aqueous condensate to obtain a water vapor stream having a temperature T 1 and a pressure p 1 a heat exchanger for, and one or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3, connected in series, of a water vapor stream having a temperature T 1 and a pressure p 1 compressing the water vapor stream to obtain a compressed water vapor stream having a temperature T 2 and a pressure p 2 means, preferably at least one, for example 1 or 2, preferably 1 heat pump compressor, each heat pump compressor including one or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 compression stages connected in series, a heat pump compressor, means, and a pressure p 2 using the compressed water vapor stream having for energy recovery, thereby obtaining a stream containing an aqueous condensate, means for, and means for transporting the water vapor stream from the heat exchanger to the means for compressing the first water vapor stream, and optionally, means for transporting the compressed water vapor stream from one upstream means for compressing the water vapor stream to the next downstream means for compressing the water vapor stream among a series of means for compressing the water vapor stream, and a pressure p 2A compressed steam stream having is transported from the last means of a series of means for compressing the steam stream to means for using the compressed steam stream having a temperature T 2 and a pressure p 2 for energy recovery, and means for transporting the compressed steam stream having a temperature T and a pressure p to means for using the compressed steam stream for energy recovery. The present invention relates to a facility including

[0052] The facility can be any type of facility in which a high-temperature fluid stream is generated and can be used for energy recovery. Non-limiting examples are, for example, industrial manufacturing sites such as chemical manufacturing sites, especially polymerization manufacturing sites, power generation facilities, facilities including engines or electronic devices or housings

[0053] The facility is preferably adapted to all aspects and embodiments of the method of the present invention for recovering steam as described above or below

[0054] In the case of a chemical manufacturing site, the facility preferably further includes means for manufacturing chemical products such as one or more reactors Furthermore, the facility preferably includes means for post-treatment of the manufacture of chemical products such as means for purifying chemical products and / or means for formulating chemical products, or other means required for treating and finishing chemical products Still further, the facility preferably includes means for transporting educts, products and / or other components used in the chemical manufacturing process to means for manufacturing chemical products, from means for manufacturing chemical products to means for post-treatment of the manufacture of chemical products, and to each means for the process steps therebetween

[0055] In the above polymerization process, the means for manufacturing chemical products preferably includes a polymerization reactor The polymerization reactor may be one polymerization reactor or a plurality of polymerization reactors connected in series One polymerization reactor can be selected from a slurry-phase reactor, for example a loop reactor, and a gas-phase reactor, for example a fluidized-bed gas-phase reactor The plurality of polymerization reactors are preferably two or more polymerization reactors, preferably 2 to 6 polymerization reactors, for example, 2, 3, 4, 5 or 6 polymerization reactors are connected in series. The plurality of polymerization reactors are usually selected from slurry phase reactors, such as loop reactors, and gas phase reactors, such as fluidized bed gas phase reactors.

[0056] The means for treating the polymer powder downstream of at least one polymerization reactor preferably includes means for separating the polymer from unreacted monomers, comonomers and other components of the product stream. Furthermore, the means for treating the polymer powder downstream of at least one polymerization reactor preferably includes means for compounding the polymer, such as an extruder.

[0057] The facility includes at least one heat exchanger. The facility can include at least one set of a plurality of heat exchangers, for example, at least two heat exchangers connected in series. The number of sets of at least two heat exchangers connected in series can be 1 to 10, for example, 1, 2, 3, 4, 5 or 6. A set of at least two heat exchangers connected in series can include two or more, for example, 2 to 6, preferably 2, 3 or 4, most preferably 2 heat exchangers connected in series.

[0058] At the polymerization production site, the number of sets of at least two heat exchangers connected in series usually depends on the number of polymerization reactors and the number of means for treating the polymer powder downstream of at least one polymerization reactor. One set of at least two heat exchangers connected in series can be connected to each polymerization reactor of the production facility and / or means for treating the polymer powder downstream of at least one polymerization reactor, preferably means for compounding the polymer, such as an extruder.

[0059] The device includes means for compressing a steam stream having one or more, preferably 1 to 5, more preferably 2 to 4, and most preferably 2 or 3 temperatures T 1 and pressures p 1 to obtain a compressed steam stream having a pressure p 2 . One or more means for compressing the steam stream are preferably connected in series. One or more means for compressing the steam stream are preferably one or more, for example 1 or 2, and preferably 1 heat pump compressor. Each heat pump compressor preferably includes 1 to 5, more preferably 2 to 4, and most preferably 2 or 3 compression stages connected in series. One or more, for example 1 or 2, and preferably 1 heat pump compressor is preferably part of one or more heat pumps known in the art.

[0060] The device further includes means for using the compressed steam stream having a pressure p 2 for energy recovery. This means for using the compressed steam stream for energy recovery can be means for using the compressed steam stream as a heating medium. In an industrial manufacturing site, the means for using the steam stream as a heating medium can be means for heating a product stream, any other stream, or a part of a component of the manufacturing site at any stage of the industrial production process or even in the heating system of the manufacturing equipment. Such means can be a heat exchanger, a reboiler, or a heating system. The means for energy recovery can be means for temporarily storing a high-temperature and / or high-pressure stream before use. Means for using the compressed water vapor stream for energy recovery are means for thermal energy storage, for example, those commercialized by Qpinch, and may be means for applying a method using a reverse condensation reaction such as a chemical heat pump, as described, inter alia, in WO 2014 / 016405 A1 pamphlet.

[0061] The means for transporting the water vapor stream from the heat exchanger to the first means for compressing the water vapor stream is preferably a pipe for connecting the means for transporting the water vapor stream from the heat exchanger to the first means for compressing the water vapor stream. The heat exchanger is preferably directly connected to the first means for compressing the water vapor stream by means for transporting the water vapor stream from the heat exchanger to the first means for compressing the water vapor stream. In this regard, "directly connected" means that the means is not connected to any further means for manipulating the temperature or pressure of the water vapor stream.

[0062] When a plurality of means for compressing the water vapor stream are connected in series, the facility includes means for transporting the compressed water vapor stream from one upstream means for compressing the water vapor stream to the next downstream means for compressing the water vapor stream in a series of means for compressing the water vapor stream. Preferably, the means for transporting the compressed water vapor stream from one upstream means for compressing the water vapor stream to the next downstream means for compressing the water vapor stream is preferably a pipe for connecting one upstream means for compressing the water vapor stream to the next downstream means for compressing the water vapor stream. Preferably, in a series of means for compressing a steam stream, each upstream means for compressing the steam stream is connected to the next downstream means for compressing the steam stream via means for transporting the compressed steam stream from one upstream means for compressing the steam stream to the next downstream means for compressing the steam stream. The upstream and next downstream means for compressing the steam stream can be directly connected via means for transporting the compressed steam stream from one upstream means for compressing the steam stream to the next downstream means for compressing the steam stream. By "directly connected" in this regard is meant that the means is not connected to any further means for manipulating the temperature or pressure of the steam stream.

[0063] However, it is preferred that the facility further comprises means for cooling the compressed steam stream downstream of at least one means for compressing the steam stream, preferably each means. At least one means for compressing the steam stream, preferably the means for cooling the compressed steam stream downstream of each means, preferably combines the compressed steam stream with a higher-pressure aqueous condensate and a portion of the aqueous condensate obtained from means for using the compressed steam stream having, for example, a pressure p 2 for energy recovery. At least one means for compressing the steam stream, preferably a suitable means for cooling the compressed steam stream downstream of each means, is most preferably a superheat reducer as known in the art.

[0064] The facility also includes means for transporting the compressed steam stream having a pressure p 2 from the last means of a series of means for compressing the steam stream to means for using the compressed steam stream having a pressure p 2 for energy recovery. Pressure p 2 A compressed steam stream having a pressure p from the last means of a series of means for compressing the steam stream to a pressure p 2 The means for transporting a compressed steam stream having a pressure p to means for use in energy recovery is preferably a pressure p 2 The last means of a series of means for compressing a compressed steam stream having a pressure p to a pressure p 2 A pipe for connecting, preferably directly connecting, the last means of a series of means for compressing a compressed steam stream having a pressure p to means for using the compressed steam stream for energy recovery. By "directly connecting" in this context is meant that the means is not connected to any further means for manipulating the temperature or pressure of the compressed steam stream having a pressure p 2

[0065] The facility is · Means for separating a second steam stream and an aqueous condensate from a stream containing the aqueous condensate obtained from means for using a compressed steam stream, · Means for transporting a stream containing an aqueous condensate from means for using a compressed steam stream to means for separating a second steam stream and an aqueous condensate from the stream containing the aqueous condensate, · Means for transporting the second steam stream from means for separating the second steam stream and the aqueous condensate to means for cooling a downstream compressed steam stream from a first (initial) upstream means for compressing the steam stream It is further preferably included.

[0066] The means for separating a second steam stream and an aqueous condensate from a stream containing the aqueous condensate obtained from means for using a compressed steam stream may be any means suitable for separating a liquid stream from a gaseous stream, for example, a vapor-liquid separator as known in the art.

[0067] ​Means for transporting a stream containing an aqueous condensate from means for using a compressed steam stream for energy recovery to means for separating a second steam stream and an aqueous condensate from the stream containing the aqueous condensate is preferably a pipe for connecting, preferably directly connecting, the means for using the compressed steam stream for energy recovery to the means for separating the second steam stream and the aqueous condensate from the stream containing the aqueous condensate. In this regard, "directly connecting" means that the means is not connected to any further means for manipulating the temperature or pressure of the stream containing the aqueous condensate.

[0068] Means for transporting a second steam stream from means for separating the second steam stream and an aqueous condensate to means for cooling a downstream compressed steam stream from an upstream first means for compressing the steam stream is preferably a pipe for connecting, preferably directly connecting, the means for separating the second steam stream and the aqueous condensate to the means for cooling the downstream compressed steam stream from the upstream first means for compressing the steam stream. In this regard, "directly connecting" means that the means is not connected to any further means for manipulating the temperature or pressure of the second steam stream.

[0069] The manufacturing equipment preferably further includes means for transporting a stream containing an aqueous condensate from means for using a compressed steam stream for energy recovery to a heat exchanger for transferring heat from a high-temperature fluid stream in a chemical manufacturing process to the aqueous condensate of the stream containing the aqueous condensate. The means for transporting a stream containing an aqueous condensate from means for using a compressed steam stream for energy recovery to a heat exchanger for transferring heat from a high-temperature fluid stream to the aqueous condensate of the stream containing the aqueous condensate is preferably a pipe for connecting, preferably directly connecting, the means for using a compressed steam stream for energy recovery to the heat exchanger for transferring heat from a high-temperature fluid stream in a chemical manufacturing process to the aqueous condensate of the stream containing the aqueous condensate. Here, "directly connecting" means that the means is not connected to any further means for manipulating the temperature or pressure of the stream containing the aqueous condensate.

[0070] Thereby, the means for transporting a stream containing an aqueous condensate preferably passes through means for separating a second steam stream and an aqueous condensate from the stream containing the aqueous condensate obtained from the means for using a compressed steam stream for energy recovery.

[0071] Use In a further aspect, the present invention relates to means for compressing one or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3, steam streams connected in series, preferably at least one, for example 1 or 2, preferably 1 heat pump compressor, each heat pump compressor including one or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 compression stages connected in series, for compressing a steam stream having a pressure p 1 to a temperature T for direct energy recovery 2 and a pressure p 2Relates to the use of the above or both of the following methods or manufacturing facilities to obtain a compressed water vapor stream having

[0072] One or more means for heating and compressing a water vapor stream, connected in series according to the present invention as described above or below, and all aspects and embodiments of the method or manufacturing facility are preferably applicable to the use of the present invention.

[0073] Detailed description of the drawings and proposed examples Figure 1 shows a schematic diagram of a prior art heat recovery stage from a fluidized bed gas phase reactor in which heat is transferred from a circulating gas stream to a working fluid in a heat exchange process. The heat of the working fluid is used to vaporize an aqueous condensate to obtain a water vapor stream for further use in a polymerization process. To increase heat recovery, the working fluid is subjected to a heating and compression process, in which the working fluid is first preheated in a preheater and then further heated and compressed in a heat pump compressor. As a result, more energy can be transferred to the aqueous condensate, and the resulting water vapor has a higher temperature and pressure. However, since the heat transfer process is always associated with energy losses due to sub-optimal heat transfer, a more efficient method of water vapor recovery is needed.

[0074] Figure 2 shows a schematic diagram of one embodiment of the method of the present invention in which heat is transferred from a high temperature fluid stream at any stage of a chemical manufacturing process to an aqueous condensate in a heat exchanger such as a waste heat boiler, and the aqueous condensate is vaporized to obtain a water vapor stream. The high temperature fluid stream before entering the heat exchanger usually has a temperature of 40 to 140 °C. The aqueous condensate preferably has a temperature of 80 to 99 °C and a high pressure of about 5 to 8 bar(a) before entering the heat exchanger. During heat transfer, the aqueous condensate is vaporized and has a temperature T of 40 to 134 °C 1 and a pressure p of 0.06 to 3 bar(a) 1A steam stream having [it] is obtained. This steam stream is subjected to two subsequent compression steps in two subsequent heat pump compressors, in which steps a compressed steam stream having a temperature and pressure in the range of 150 to 300 °C and 4 to 10 bar(a) is obtained, whereby direct use of the compressed steam stream in the chemical manufacturing process becomes possible. After the first and second compression steps, if the temperature of the steam stream exceeds 300 °C, the temperature of the steam stream can be reduced in a superheat reducer by introducing a portion of an aqueous condensate stream having temperature T 1 and pressure p 1 . After use in the chemical manufacturing process, the steam stream is usually condensed and reused for heat transfer. Therefore, the aqueous condensate cycle includes a valve for guiding excess steam to an external user and introducing external steam as needed. The steam stream introduced into the steam user within the manufacturing process has a temperature T 2 in the range of 144 to 180 °C and a pressure p 2 of 4 to 10 bar(a). After use, the steam stream is partially or completely condensed and has a temperature of 80 to 99 °C and a pressure of 1 bar(a). The condensed stream is collected in a condensate collector. In order to reuse the aqueous condensate in heat transfer, the pressure of the aqueous condensate is increased to 5 to 8 bar(a) as described above.

[0075] Figure 3 shows a schematic diagram of another embodiment of the method of the present invention in which the condensed steam stream after use in the chemical manufacturing process is separated into a second steam stream having a temperature of 100 to 121 °C and a pressure of 1.01 to 2 bar(a) and an aqueous condensate. The aqueous condensate is reused for heat transfer, while the second steam stream is combined with the heated and compressed steam stream after the first heating and compression steps.

[0076] Figure 4 shows a proposed example of the embodiment of Figure 2. This example has been proposed using ASPEN Plus. An aqueous condensate stream (S1) having a temperature of 80°C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 12000 kg / hr is subjected to a heat exchange process for cooling a high-temperature fluid stream in a heat exchanger. The aqueous condensate stream is vaporized into a steam stream (S2) having a temperature of 65°C, a pressure of 0.23 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 12000 kg / hr. The steam stream is subjected to a first compression process in the first compression stage of a heat pump compressor such that the steam stream has a temperature of 234°C, a pressure of 1 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 12000 kg / hr (S4). To cool the steam stream, the steam stream is combined with a higher-pressure aqueous stream in a first superheat reducer. The higher-pressure aqueous stream has a temperature of 80°C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 1300 kg / hr (S6). After the first superheat reducer, the cooled steam stream has a temperature of 106°C, a pressure of 1 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 13300 kg / hr (S5). This cooled steam stream is subjected to a second compression process in the second compression stage of a heat pump compressor such that the steam stream has a temperature of 198°C, a pressure of 2 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 13300 kg / hr (S8). To cool the steam stream, the steam stream is combined with a higher-pressure aqueous stream inside a second superheat reducer. The higher-pressure aqueous stream has a temperature of 80°C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 850 kg / hr (S13). After the second superheat reducer, the cooled steam stream has a temperature of 125°C, a pressure of 2 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 14150 kg / hr (S9). This cooled steam stream is subjected to a third compression process in the third compression stage of a heat pump compressor such that the steam stream has a temperature of 197°C, a pressure of 4 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 14150 kg / hr (S10).To cool the steam stream, the steam stream is combined with a higher-pressure aqueous stream in a third superheat reducer. The higher-pressure aqueous stream has a temperature of 80 °C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 650 kg / hr (S11). After the third superheat reducer, the cooled steam stream has a temperature of 146 °C, a pressure of 4 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 14,800 kg / hr (S9). The compressed steam stream can be used for energy recovery.

[0077] Figure 5 shows a proposed example of the embodiment of Figure 3. This example has been proposed using ASPEN Plus. An aqueous condensate stream (S1) having a temperature of 80°C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 11260 kg / hr is subjected to a heat exchange process for cooling a high-temperature fluid stream in a heat exchanger. This aqueous condensate stream is vaporized into a steam stream (S2) having a temperature of 65°C, a pressure of 0.23 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 11260 kg / hr. This steam stream is subjected to a first compression process in the first compression stage of a heat pump compressor such that the steam stream has a temperature of 234°C, a pressure of 1 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 11260 kg / hr (S4). To cool the steam stream, this steam stream is combined with a higher-pressure aqueous stream in a first superheat reducer. The higher-pressure aqueous stream has a temperature of 80°C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 1200 kg / hr (S6). In addition, a second steam stream (S7) having a temperature of 101°C, a pressure of 1 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 840 kg / hr is introduced into the first superheat reducer and combined with the other two streams. After the first superheat reducer, the cooled steam stream has a temperature of 107°C, a pressure of 1 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 13300 kg / hr (S5). The above-cooled steam stream is subjected to a second compression process in the second compression stage of a heat pump compressor such that the steam stream has a temperature of 200°C, a pressure of 2 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 13300 kg / hr (S8). To cool the steam stream, the steam stream is combined with a higher-pressure aqueous stream within a second superheat reducer. The higher-pressure aqueous stream has a temperature of 80°C, a pressure of 7 bar(a), a steam fraction of 0 wt%, and a mass flow rate of 850 kg / hr (S13). After the second superheat reducer, the cooled steam stream has a temperature of 127°C, a pressure of 2 bar(a), a steam fraction of 100 wt%, and a mass flow rate of 14150 kg / hr (S9).This cooled water vapor stream is subjected to a third compression step in the third compression stage of the heat pump compressor such that the water vapor stream has a temperature of 198 °C, a pressure of 4 bar(a), a vapor fraction of 100 wt%, and a mass flow rate of 14150 kg / hr (S10). To cool the water vapor stream, the water vapor stream is combined with a higher-pressure aqueous stream in a third superheat reducer. The higher-pressure aqueous stream has a temperature of 80 °C, a pressure of 7 bar(a), a vapor fraction of 0 wt%, and a mass flow rate of 650 kg / hr (S11). After the third superheat reducer, the cooled water vapor stream has a temperature of 148 °C, a pressure of 4 bar(a), a vapor fraction of 100 wt%, and a mass flow rate of 14800 kg / hr (S9). This compressed stream is further used for heat exchange in a second heat exchanger where the compressed stream is condensed. The resulting aqueous condensate stream has a temperature of 144 °C, a pressure of 4 bar(a), a vapor fraction of 0 wt% and a mass flow rate of 14800 kg / hr (S3) and can be used for energy recovery.

[0078] The proposed process as shown in FIGS. 4 and 5 has the following energy consumption Q (load [kW]) and W (power [kW]), and coefficient of performance (COP) which is the ratio of the power consumption W to the generated water vapor as shown in Table 1.

[0079]

Table 1

Claims

1. An energy recovery method, comprising: a) supplying a high-temperature fluid stream; b) thermally contacting the high-temperature fluid stream with the aqueous condensate in the heat exchanger, thereby transferring heat from the high-temperature fluid stream to the aqueous condensate and vaporizing at least a portion of the aqueous condensate to obtain a steam stream having a temperature T １ and a pressure p １ ; and c) subjecting the steam stream to at least one, for example 1 to 5, preferably 2 to 4, most preferably 2 to 3 compression steps to obtain a compressed steam stream having a pressure p ２ and a step of obtaining a compressed steam stream having a pressure p d) using the compressed water vapor stream for energy recovery to obtain a stream containing an aqueous condensate; and comprising: In the at least one compression step c), the temperature of the water vapor stream is raised to temperature T ２ and Temperature T ２ is 50 K to 250 K, preferably 65 K to 150 K, most preferably 75 K to 125 K higher than the temperature T １ and Pressure p １ The pressure p with respect to ２ the ratio of p ２ / p １ is 5 to 50, method.

2. The high-temperature fluid stream has a temperature T of 20 to 150 °C, more preferably 25 to 130 °C, and most preferably 30 to 110 °C ｆ The method according to claim 1, which has the above characteristics.

3. The aqueous condensate has a temperature T of 40°C to 99°C, preferably 50°C to 98°C, most preferably 55°C to 95°C ｃ , and / or a pressure p of 1 to 10 bar(a), preferably 2 to 9 bar(a), most preferably 3 to 8 bar(a) ｃ The method according to claim 1 or claim 2 having the above.

4. Temperature T １ is in the range of 30°C to 150°C, preferably 40°C to 135°C, most preferably 50°C to 100°C, and / or the pressure p １ is in the range of 0.04 bar(a) to 4.76 bar(a), preferably 0.07 to 3.13 bar(a), most preferably 0.12 to 1.01 bar(a). The method according to any one of claims 1 to 3

5. In said at least one compression step c), the temperature of said heated first heat transfer fluid is raised to temperature T ２ and temperature T ２ is in the range of 125 °C to 300 °C, preferably 135 °C to 275 °C, most preferably 140 °C to 250 °C, and / or the pressure p ２ is in the range of 3 bar(a) to 12 bar(a), preferably 4 to 10 bar(a), most preferably 5 to 8 bar(a), according to any one of claims 1 to 4.

6. The method according to any one of claims 1 to 5, wherein the temperature of the compressed water vapor stream does not exceed 300 °C, and preferably the temperature of the compressed water vapor stream after each compression step is reduced after one or more compression steps.

7. The method according to claim 6, wherein the temperature of the compressed water vapor stream after each compression step is reduced by combining the compressed water vapor stream with an aqueous condensate at a higher pressure, preferably a portion of the aqueous condensate in step d), preferably in a superheat reducer.

8. The method according to any one of claims 1 to 7, wherein the aqueous condensate obtained from the used heated and compressed water vapor stream is used to bring the high-temperature fluid stream into thermal contact with the aqueous condensate in a first heat exchanger.

9. The method according to any one of claims 1 to 8, wherein the stream containing the aqueous condensate obtained from the compressed water vapor stream used for heat recovery is subjected to a vapor separation step to obtain a second water vapor stream and an aqueous condensate, and the second water vapor stream is preferably combined with the compressed water vapor stream after the first compression step.

10. The steam stream is subjected to the compression stage of the heat pump compressor in each compression step to obtain a compressed steam stream having a pressure p ２ The method according to any one of claims 1 to 9, wherein a compressed steam stream having ２ is obtained.

11. Equipment for recovering energy, comprising: Transfer heat from a high-temperature fluid stream to an aqueous condensate to obtain a steam stream having a temperature T １ and a pressure p １ and a heat exchanger for obtaining a steam stream having a pressure p One or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3, temperatures T connected in series １ and pressures p １ Compress the steam stream having to obtain a compressed steam stream having temperature T ２ and pressure p ２ Means for obtaining, preferably at least one, for example one or two, preferably one heat pump compressor, each heat pump compressor having one or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 compression stages connected in series, a heat pump compressor, means Pressure p ２ means for using said compressed water vapor stream having Pressure p for energy recovery to thereby obtain a stream containing aqueous condensate; means for transporting the water vapor stream from the heat exchanger to an upstream first means for compressing the water vapor stream; optionally, means for transporting the compressed water vapor stream from one upstream means for compressing the water vapor stream to the next downstream means for compressing the water vapor stream among a series of said means for compressing the water vapor stream; pressure p ２ transporting the compressed steam stream having the pressure p from the last of the series of means for compressing the steam stream to the means for using the compressed steam stream having the pressure p for energy recovery ２ and means for and comprising a manufacturing facility.

12. Means for cooling the compressed steam stream downstream of each means for compressing the steam stream, preferably combining the heated and compressed steam stream with a higher-pressure aqueous condensate and, for example, a portion of the aqueous condensate obtained from said means for using the compressed steam stream having pressure p ２ Means for combining, most preferably a superheat reducer, with a portion of the aqueous condensate obtained from said means for using the compressed steam stream for energy recovery The manufacturing facility according to claim 11, further comprising:

13. means for separating a second water vapor stream and an aqueous condensate from the stream containing the aqueous condensate obtained from the means for using the compressed water vapor stream. means for transporting a stream containing the aqueous condensate from the means for using the compressed steam stream for energy recovery to the means for separating a second steam stream and an aqueous condensate from the stream containing the aqueous condensate; means for transporting the second steam stream from the means for separating the second steam stream and the aqueous condensate to the means for cooling the compressed steam stream downstream from the first upstream means for compressing the steam stream; The manufacturing facility according to claim 12, further comprising. **Claim 14** means for transporting a stream containing the aqueous condensate from the means for using the compressed steam stream for energy recovery to the heat exchanger for transferring heat to the aqueous condensate of the stream containing the aqueous condensate from a high-temperature fluid stream; The manufacturing facility according to any one of claims 11 to 13, further comprising, wherein the means for transporting the stream containing the aqueous condensate preferably passes through the means for separating a second steam stream and an aqueous condensate from the stream containing the aqueous condensate obtained from the means for using the compressed steam stream for energy recovery. **Claim 15** One or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 means for compressing a steam stream, preferably at least one, for example 1 or 2, preferably 1 heat pump compressor, each heat pump compressor being a heat pump compressor comprising one or more, preferably 1 to 5, more preferably 2 to 4, most preferably 2 or 3 compression stages connected in series, of the means, at a temperature T １ and a pressure p １ Compressing a steam stream having to obtain a compressed steam stream having a pressure p for direct energy recovery, use in a method according to any one of claims 1 to 10 or a manufacturing facility according to any one of claims 11 to 14. ２ ​

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