WO2026008293A1 - Process and plant arrangement for the production of polytetrahydrofuran (poly-thf) - Google Patents

Process and plant arrangement for the production of polytetrahydrofuran (poly-thf)

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Publication number
WO2026008293A1
WO2026008293A1 PCT/EP2025/066698 EP2025066698W WO2026008293A1 WO 2026008293 A1 WO2026008293 A1 WO 2026008293A1 EP 2025066698 W EP2025066698 W EP 2025066698W WO 2026008293 A1 WO2026008293 A1 WO 2026008293A1
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WO
WIPO (PCT)
Prior art keywords
thf
evaporator
water
vapor stream
fed
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/EP2025/066698
Other languages
French (fr)
Inventor
Sachin Kumar ARORA
Marcel Horn
Stefanie Maria VIGNESH
Jakob PATZ
Marco SCHOENWALD
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BASF SE
Original Assignee
BASF SE
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Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of WO2026008293A1 publication Critical patent/WO2026008293A1/en
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/04—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers only
    • C08G65/06—Cyclic ethers having no atoms other than carbon and hydrogen outside the ring
    • C08G65/16—Cyclic ethers having four or more ring atoms
    • C08G65/20—Tetrahydrofuran
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/06—Flash distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/36—Azeotropic distillation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
    • C08G65/2696—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds characterised by the process or apparatus used
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/30—Post-polymerisation treatment, e.g. recovery, purification, drying
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/34—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from hydroxy compounds or their metallic derivatives
    • C08G65/46—Post-polymerisation treatment, e.g. recovery, purification, drying

Definitions

  • the present invention relates to a process and plant arrangement for the production of polytetrahydrofuran (poly-THF).
  • poly-THF polytetrahydrofuran
  • Polytetrahydrofuran is a polymer consisting of the monomeric unit [O- CH2-CH2-CH2-CH2] and can be described with the chemical formula HO-((CH 2 )4O)nH. Accordingly, poly-THF is a mixture of polyether diols terminated with alcohol groups. Poly-THF is widely used as a starting material for making elastic fibres, polyurethane resins, thermoplastic polyurethane, thermoplastic polyesters, polyetheramide and cast polyurethane elastomers, used for instance in the wheels of roller skates and skateboards.
  • poly-THF polytetrahydrofuran
  • THF intermediate tetrahydrofuran
  • the obtained and optionally purified intermediate compound THF is than used as starting material in a polymerization reaction to form poly-THF.
  • One of the main reaction routes relies on a reaction of THF with acetic anhydride (AczO), followed by a step in which residual THF is removed, by a reaction step wherein MeOH (methanol) is used in a transesterification and a step wherein residual MeOH is removed.
  • AczO acetic anhydride
  • heat transfer media with a low heat content which only appear to be usable for releasing waste heat into the environment.
  • the use of heat pumps in the chemical industry is well known in this regard. With the current energy crisis and the growing pressure for decarbonization, they are also becoming an increasingly attractive option for the (large-scale) process industry.
  • a heat pump uses existing heat from a heat transfer media I heat source at a low temperature level and brings it to a higher temperature level using electricity and a refrigerant or the like workingfluid. Accordingly, a suitable heat source is the basic requirement for using a heat pump. In principle, different concepts come into consideration for this. However, there are restrictions to be accounted for in large- scale chemical processes.
  • heat sources to be considered are: (waste) air or (waste) water, the ground, refrigeration systems or cooling systems, combined heat of power plants or from compressed air generation and, in this case, waste heat from production processes.
  • temperatures of just a few degrees plus are sufficient, so that previously unused waste heat can in principle be made usable with a heat pump.
  • the aim should at least be to enable the steam level that can be achieved with a heat pump to be used in e.g. chemical processes and a certain efficiency should also be given.
  • the efficiency is in most cases, also here, determined via the COP value (“Coefficient of Performance” - in German also known as “jit- siere”) as a measure of the efficiency of a heat pump.
  • a COP below 3 usually indicates that a heat pump can only work sub optimally.
  • the COP is determined under laboratory conditions and only relates to the heat pump, not to the peripherals. However, which COP value is considered good varies depending on the specific application and the type of heat pump. In some cases lower COP are thus also acceptable.
  • poly-THF polytetrahydrofuran
  • the present invention concerns in its categories a process for the production of poly- THF and a plant arrangement designed for the production of poly-THF. Embodiments, aspects or features disclosed for or in connection with one of these categories in each case analogously apply for the other categories of the invention.
  • the present invention relates to a process for the production of polytetrahydrofuran (poly-THF), wherein
  • poly-THF polytetrahydrofuran
  • a first process vapor stream is fed to an inlet of the heat input side of a first evaporator of at least two evaporators
  • a second process vapor stream is fed to an inlet of the heat input side of a second evaporator of at least two evaporators, and - the first process vapor stream and the second process vapor stream are further used or recirculated in the process from outlets of the heat input side of the first evaporator and the second evaporator, and
  • - feed water in particular demineralized water
  • demineralized water is fed to inlets of the heat output side of the first evaporator and the second evaporator for the generation of a first water steam stream on an outlet of the heat output side of the first evaporator and a second water steam on an outlet of the heat output side of the second evaporator
  • the generated first water steam stream and the generated second water steam stream downstream from the heat output sides of the first evaporator and the second evaporator are combined and fed to the inlet of a water evaporation unit, in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase, and
  • the vapor water phase downstream from the water evaporation unit is com-pressed in a compressor arrangement into compressed water vapor of a specific pressure and temperature, in particular is compressed by using electrical energy from a renewable energy source, and
  • the compressed water vapor of a specific pressure and temperature is fed into a vapor grid, in particular a heating network.
  • process vapor stream designates a vapor stream deriving from a process stage of the production of poly-THF.
  • Said process stage can be of any kind and may for example be a reaction process, a purification process, a distillation process or a removal process.
  • the process vapor streams according to the present invention are not limited to a certain chemical composition of the vapor and may comprise, starting materials, intermediates, added compounds and/or reaction products in any given ratio.
  • evaporator generally can be any kind of “heat exchanger”.
  • the evaporator is generally part of a heat pump cycle wherein the evaporated steam is provided for further use, in particular further use in an industrial steam grid.
  • the main concept of the present invention lies within the parallel utilization of thermal energy from each of the at least two process vapor streams.
  • the thermal energy of every individual process vapor stream designated as first, second, third, fourth etc. process vapor stream, is transferred to feed water in order to generate a water steam stream, designated as first, second, third, fourth etc. water steam stream.
  • Said transfer of thermal energy is conducted in individual evaporators, designated as first, second, third, fourth etc. evaporator.
  • a first process vapor stream is used as heat source to generate a first water steam stream, wherein said heat transfer is conducted in a first evaporator; in parallel a second process vapor stream is used as heat source to generate a second water steam stream, wherein said heat transfer is conducted in a second evaporator and so on.
  • the inventive concept identifies at least two process vapor streams provided downstream of the process which are suitable as heat source for heat exchangers in the form of at least two evaporators.
  • the invention utilizes the combined thermal energy of the least two process vapor streams which when taken alone might not contain enough thermal energy.
  • a relevant part of the process heat from the process vapor streams associated with the production of poly-THF is transferred to compressed water vapor of a specific pressure and temperature which is fed to a vapor grid, in particular a heating network, instead of being “wasted”.
  • heating networks of chemical production sites are currently mainly heated with fossil fuels
  • the process according to the invention improves energy efficiency and reduces emissions of greenhouse gases. Emissions of greenhouse gases are further reduced by preferably using electrical energy from a renewable energy source to run the compressor arrangement.
  • the implementation and utilization of the at least two evaporators according to the invention instead of air coolers also solves the problem of limited cooling capacity which is a bottleneck at high ambient temperature during summertime. Furthermore only a single compressor arrangement is needed to compress the combined water steam streams generated by the at least two or more evaporators which minimizes investment costs and space usage.
  • a third process vapor stream is fed to an inlet of the heat input side of a third evaporator
  • the third process vapor stream is further used or recirculated in the process from an outlet of the heat input side of the third evaporator, and
  • the generated third water steam stream downstream from the heat output side of the third evaporator is combined with the generated first and second water steam stream downstream from the heat output sides of the first and second evaporator and fed to the inlet of the water evaporation unit, in particular flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase.
  • a total number of at least three process vapor streams associated with at least three process stages of the process of producing poly-THF are provided in parallel and the combined thermal energy of said at least three process vapor streams is utilized instead of being “wasted”. This makes the process even more efficient and reduces the emission of greenhouse gases even more.
  • More preferred is a process of the present invention wherein at least four process vapor streams are provided downstream of the process and wherein - a fourth process vapor stream is fed to an inlet of the heat input side of a fourth evaporator, and
  • the fourth process vapor stream is further used or recirculated in the process from an outlet of the heat input side of the fourth evaporator, and
  • the generated fourth water steam stream downstream from the heat output side of the fourth evaporator is combined with the generated first, second and third water steam stream downstream from the heat output sides of the first, second and third evaporator and fed to the inlet of the water evaporation unit, in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase.
  • a total number of at least four process vapor streams associated with at least four process stages of the process of producing poly-THF are provided in parallel and the combined thermal energy of said at least four process vapor streams is utilized instead of being “wasted”. This makes the process even more efficient and reduces the emission of greenhouse gases even more.
  • process vapor streams provided in the process of the present invention are associated with specific individual process steps and process stages, wherein said process steps and process stages are part of the overall process of producing poly-THF. Accordingly, the inventive concept is applicable to a number of different sources of process vapor streams which makes it feasible and economically attractive.
  • the first process vapor stream of the four process vapor streams derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
  • the second process vapor stream of the four process vapor streams derives from purification step in the process stage of producing THF from 1 ,4-butanediol
  • the third process vapor stream of the four process vapor streams derives from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO), and
  • the fourth process vapor stream of the four process vapor streams derives from a methanol removal step in the process stage of producing poly-THF from THF and AC2O.
  • Said more preferred embodiment utilizes a total number of four process vapor streams, wherein each of the four individual process vapor streams is associated with one out of four process steps and process stages of the process of producing poly-THF.
  • the combined thermal energy of said four individual process vapor streams as specified above is used as heat source for the generation of four individual water steam streams, wherein the heat transfer is conducted in four individual evaporators.
  • four process vapor streams are provided in parallel and the combined thermal energy of said four process vapor streams as specified above is utilized instead of being “wasted”. This makes the process even more efficient and reduces the emission of greenhouse gases even more. It is a special achievement of the present invention to identify particularly suitable sources of process vapor streams out of the numerous options for different process steps in the process of producing poly-THF.
  • each of the process vapor streams which are utilized as heat source have a minimum temperature of at least 50 °C, preferably of at least 55 °C.
  • said defined minimum temperature ensures a certain amount of thermal energy of the at least two, preferably four, process vapor streams for the generation of the at least two, preferably four, water steam streams in the evaporators.
  • thermal energy of at least two process vapor streams is utilized in parallel, i.e. thermal energy is combined, in preferred cases the thermal energy of three, four or more process vapor streams is utilized in parallel.
  • each of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and wherein
  • the first process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
  • the second process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C derives from purification step in the process stage of producing THF from 1 ,4- butanediol
  • - the third process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C derives from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO)
  • the fourth process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, derives from a methanol removal step in the process stage of producing poly- THF from THF and acetic anhydride (AczO).
  • the inventive concept identifies suitable sources of process vapor streams which are similar in temperature.
  • Those suitable sources of process vapor streams which are similar in temperature are more preferably associated with specific individual process steps and process stages as identified above, wherein said process steps and process stages are part of the overall process of producing poly- THF.
  • process vapor streams which are similar in temperature allows for a particularly facile and effective process wherein the synergistic effect of process vapors condensing at approximately same temperatures are utilized.
  • the mode of operation and/or the design of plant elements such as pipes, valves, evaporators and the like can thus be kept simple which reduces investment and operational costs and makes the implementation of the process according to the present invention into existing processes and plant arrangements feasible.
  • pressure and temperature of the at least two, preferably four, process vapor streams provided downstream of the process are in the ranges as defined above.
  • pressure and temperature of the at least two, preferably four, process vapor streams provided downstream of the process are in the ranges as defined above and wherein the two or more, preferably four, process vapor streams provided downstream of the process derive from the process steps and process stages as defined above.
  • a particularly preferred process according to the present invention provides and utilizes the following four process vapor streams:
  • - derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
  • - has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
  • - has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara, and
  • - has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
  • - has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara, and
  • - derives from a transesterification step in the process stage of producing poly- THF from THF and acetic anhydride (AczO), and - has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
  • - has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara, and
  • - has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
  • - has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara.
  • THF tetrahydrofuran
  • the total amount of thermal energy of process vapor streams deriving from a process step in the process stage of producing THF is at least 1 .5 MW per production of 1 kg THF, preferably is at least 2 MW per production of 1 kg THF.
  • the process according to the present invention provides and utilizes a first process vapor stream deriving from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butane- diol and a second process vapor stream deriving from a purification step in the process stage of producing THF from 1 ,4-butanediol, wherein the total amount of thermal energy of the combined first and second process vapor stream is at least 1 .5 MW per production of 1 kg THF, preferably is at least 2 MW per production of 1 kg THF.
  • a distillation step preferably an azeotropic distillation
  • the total amount of thermal energy of process vapor streams deriving from a process step in the process stage of producing poly-THF is at least 1 .5 MW per production of 1 kg poly-THF, preferably is at least 2 MW per production of 1 kg poly-THF.
  • the process according to the present invention provides and utilizes a third process vapor stream deriving from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO) and a fourth process vapor stream deriving from a methanol removal step in the process stage of producing poly-THF from THF and acetic anhydride (AczO), wherein the total amount of thermal energy of the combined third and fourth process vapor stream is at least 1 .5 MW per production of 1 kg poly-THF, preferably is at least 2 MW per production of 1 kg poly-THF.
  • the process according to the present invention is characterized in that the combined mass flow of the at least two, preferably four, process vapor streams provided downstream of the process is at least 40 t/h, preferably is at least 50 t/h, more preferably is at least 60 t/h.
  • a third evaporator positioned in a third process vapor stream bypass conduit designed for bypassing a third main process vapor stream conduit, wherein the third evaporator is either fed with the third process vapor stream or is bypassed by the third process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the third evaporator in the third process vapor stream bypass conduit and in the third main process vapor stream conduit, and
  • a fourth evaporator positioned in a fourth process vapor stream bypass conduit designed for bypassing a fourth main process vapor stream conduit, wherein the fourth evaporator is either fed with the fourth process vapor stream or is bypassed by the fourth process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the fourth evaporator in the fourth process vapor stream bypass conduit and in the fourth main process vapor stream conduit.
  • Said preferred embodiment involving individual process vapor stream bypass conduits as described above allows for a certain flexibility of the process as individual evaporators are either in operation, i.e. are fed with a process vapor stream, or are not in operation, i.e. are bypassed by a process vapor stream. Accordingly, the process can react to fluctuating conditions during the process of producing poly-THF, e.g. if certain process stages or process steps are out of operation due to maintenance work or when the production capacity of the plant arrangement for the production of poly-THF or certain parts or units of the plant arrangement for the production of poly-THF is reduced.
  • a process usually operating with four evaporators in parallel might also operate with only three or two of the evaporators.
  • the process involves:
  • a first evaporator which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the first evaporator, and
  • a second evaporator which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the second evaporator, and
  • a third evaporator which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the third evaporator, and
  • a fourth evaporator which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the fourth evaporator.
  • Said preferred embodiment involving individual valves positioned in front of the inlets of the heat output side of the evaporators as described above allows for a certain flexibility of the process as individual evaporators are either fed with feed water or are bypassed by the feed water. Accordingly, the process can react to fluctuating conditions during the process of producing poly-THF, e.g. if certain process stages or process steps are out of operation due to maintenance work or when the production capacity of the plant arrangement for the production of poly-THF or certain parts or units of the plant arrangement for the production of poly-THF is reduced. Furthermore this allows for individual maintenance of individual evaporators without interrupting the overall process. E.g., a process usually operating with four evaporators in parallel might also operate with only three or two of the evaporators.
  • the first process vapor stream provided derives from a distillation process stage unit, preferably an azeotropic distillation process stage unit, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
  • the second process vapor stream provided derives from a purification process stage unit in the process stage of producing THF from 1 ,4-butanediol, and
  • the third process vapor stream provided derives from a transesterification process stage unit in the process stage of producing poly-THF from THF and acetic anhydride (AczO), and
  • the fourth process vapor stream provided derives from a methanol removal process stage unit in the process stage of producing poly-THF from THF and acetic anhydride (AC2O).
  • the process vapor streams provided in the process are associated with process stage units of the process of producing THF and/or poly- THF are in close proximity to each other, thus allowing for a cost effective and facile installation and implementation of the system I process according to the present invention.
  • Said preferred arrangement makes the parallel utilization of two, three, four or more heat sources in the form of process vapor streams feasible, minimizes loss of thermal energy in transport processes and inter alias saves piping material.
  • first preheater before the feed water is fed to the inlet of the heat output side of a first evaporator wherein the first preheater utilizes a first process vapor stream exiting the first evaporator as heating medium, and/or, preferably “and”
  • a third preheater before the feed water is fed to the inlet of the heat output side of a third evaporator wherein the third preheater utilizes a third process vapor stream exiting the third evaporator as heating medium, and/or, preferably “and”
  • a fourth preheater before the feed water is fed to the inlet of the heat output side of a fourth evaporator wherein the fourth preheater utilizes a fourth process vapor stream exiting the fourth evaporator as heating medium.
  • the present invention relates to a plant arrangement designed for the production of poly-THF, comprising
  • a water evaporation unit in particular a flash drum, downstream from the heat output sides of the at least two evaporators which is designed
  • plant arrangement designates a chemical production site which comprises several individual plant units and which can be subdivided in two or more plant sectors.
  • the plant sectors are distinguished with regard to their target product, i.e. a first plant sector produces THF and a second plant sector produces poly-THF.
  • a first plant sector produces THF
  • a second plant sector produces poly-THF.
  • the individual plant units and sectors of said plant arrangement are in close proximity to each other, more preferably all parts of the plant arrangement are within the same building.
  • water evaporation unit designates a construction or process or plant unit or the like feature capable of performing evaporation -full evaporation or partial evaporation- to a water steam, preferably at least in part by flash evaporation, in order to produce a vapor water phase and a liquid water phase by means of a partial evaporation, possibly only a liquid water phase by means of a full evaporation.
  • Flash evaporation occurs when a water steam stream undergoes a reduction in pressure by passing through a throttling valve or other throttling device.
  • the water evaporation unit is a flash drum wherein a throttling valve or device is located at the entry into a pressure vessel so that the flash evaporation occurs within the vessel.
  • compressor arrangement designates a construction/process/plant unit capable of compressing a vapor phase to a certain pressure and temperature level.
  • Said compressor arrangement may consist of a single compressor or may comprise two or more compressors each in a compressor stage of the compressor arrangement, respectively a compressor unit or units.
  • Compressor stages may preferably be arranged in the form of a compressor cascade of compressors or compressor units, e.g. three compressors or compressor units in a row as shown in an embodiment of Fig. 7.
  • a compressor may preferably be combined with another element such as a valve, a spray nozzle or the like element supporting compressing of the vapor phase to a certain pressure and temperature level; said element may be arranged as an intermediate element between a first and a second compressor of a compressor arrangement.
  • another element such as a valve, a spray nozzle or the like element supporting compressing of the vapor phase to a certain pressure and temperature level; said element may be arranged as an intermediate element between a first and a second compressor of a compressor arrangement.
  • An individual compressor preferably is a steam compressor of specific kind, namely in the form of a screw compressor, a radial fan or an axial turbo compressor.
  • a combination of different kinds of compressors is possible in said compressor arrangement. More preferably all compressors in said compressor arrangement are steam compressors of the same kind, namely either in the form of a screw compressor or alternatively a radial fan or alternatively an axial turbo compressor.
  • Water is usually added to spray off the live steam after the compressor with the longest possible inlet section. Ideally, the water is sprayed to support or even accelerate evaporation and to avoid the formation of droplet streaks.
  • Preferably all compressor stages each combines a spray nozzle with the compressor to provide a compressor unit.
  • At least one or some, preferably all of the compressor stages are driven with electrical power from regenerative energy sources.
  • all power consumptions explained above is generated green, i.e. the power is generated from regenerative electrical energy sources like wind, solar or the like “green” energy sources.
  • a first evaporator in the first plant sector designed to be fed by the first process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a first water steam stream at the outlet of the heat output side, and
  • a second evaporator in the first plant sector designed to be fed by the second process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a second water steam stream at the outlet of the heat output side, and
  • a third evaporator in the second plant sector designed to be fed by the third process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a third water steam stream at the outlet of the heat output side, and
  • a fourth evaporator in the second plant sector designed to be fed by the fourth process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a fourth water steam stream at the outlet of the heat output side, and
  • a water evaporation unit in particular a flash drum, downstream from the heat output sides of the first, second, third and fourth evaporator which is designed to be fed by the combined first, second, third and fourth water steam streams from the outlets of the first, second, third and fourth evaporator.
  • one, two or more, preferably all, of the at least two, preferably four, separate sources of process vapor streams in the first and/or second plant sector are reactors or columns, preferably rectification columns.
  • transesterification unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO,
  • the plant arrangement according to the present invention comprises four separate sources of process vapor streams, wherein - the first source of process vapor stream providing a first process vapor stream is a distillation unit in the first plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material, and
  • the second source of process vapor stream providing a second process vapor stream is a purification unit in the first plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material, and
  • the third source of process vapor stream providing a third process vapor stream is a transesterification unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO, and
  • the fourth source of process vapor stream providing a fourth process vapor stream is a methanol removal unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO.
  • the plant arrangement comprises four evaporators, wherein each of the four evaporators is designed to be fed by feed water at the inlet of the heat output side of the evaporator and to eject a water steam stream at the outlet of the heat output side of the evaporator, and wherein
  • the first evaporator is designed to be fed by the first process vapor stream at the inlet of the heat input side
  • the second evaporator is designed to be fed by the second process vapor stream at the inlet of the heat input side
  • the third evaporator is designed to be fed by the third process vapor stream at the inlet of the heat input side
  • the fourth evaporator is designed to be fed by the fourth process vapor stream at the inlet of the heat input side.
  • the plant arrangement according to the present invention additionally comprises one, two or more or all of the following plant components (units) - a recirculation conduit designed to recirculate the liquid water phase from the water evaporation unit as feed water to the inlets of the heat output sides of the at least two evaporators,
  • preheaters for preheating the feed water before it is fed to the inlet of the heat output side of the at least two evaporators, wherein the preheaters are designed to utilize the at least two process vapor streams exiting the at least two evaporators as heating medium,
  • the present invention further relates to a target product that can be obtained or achieved by a method according to the present invention.
  • Reference RF1 The publication Prior Art Disclosure; Issue 684; paragraphs [1000] to [8005]; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety.
  • the target product is a product as described in Reference RF1 ; paragraphs [1000] to [8005].
  • the process described herein is further a process for the production of a product, preferably a target product.
  • the converting step to obtain the target product preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art.
  • the converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and/or steam cracking; and/or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and/or subjecting to ion exchanger; and/or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and/or compounding; and/or forming, preferably foaming, extruding and/or molding; and/or finishing, preferably coating and/or smoothing.
  • step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and/or steam cracking; and/or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and/or subjecting to ion exchanger; and/or assembling,
  • the term “building block”, as used herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and/or higher molecular weight than the building block on which the secondary product is based.
  • the building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds.
  • the alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.
  • the term “monomer”, as used herein, comprises molecules, which can react with each other to form polymer chains by polymerization.
  • the monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates.
  • (Meth)acrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms.
  • (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable.
  • the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.
  • the building block can further be an intermediate compound.
  • intermediate compound comprises organic reagents, which are applied for formation of compounds with higher molecular complexity.
  • the intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide.
  • the polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and/or diphenylmethane diisocyanate (MDI).
  • TDI toluene diisocyanate
  • MDI diphenylmethane diisocyanate
  • polymer A comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs [2001 ] to [2007] of Reference RF1 .
  • polymer composition A comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and/or flame retardant, and is defined in more detail in paragraph [2008] of Reference RF1 .
  • polymer product A comprises any product comprising the polymer A and/or polymer composition A as described above and is defined in more detail in paragraphs [2009] and [2010] of Reference RF1 .
  • the step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is/are described in more detail in paragraph [201 1 ] of Reference RF1 .
  • the term “industrial use polymer”, as used herein, comprises rheology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs [3035] to [3044] of Reference RF1 .
  • industrial use surfactant comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs [3008] to [3034] of Reference RF1 .
  • the term “industrial use descaling compound”, as used herein, comprises nonphosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs [3001 ] to [3005] of Reference RF1 .
  • the term “industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs [3006] to [3007] of Reference RF1 .
  • the term “industrial use solvent”, as used herein, comprises alkyl amides, alkyllactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs [3045] to [3055] of Reference RF1 .
  • the term “industrial use dispersant”, as used herein, comprises anionic and nonionic industrial use dispersants defined in more detail in paragraphs [3056] to [3058] of Reference RF1 .
  • composition and/or formulation thereof” with reference to the industrial use polymers, industrial use surfactants, descaling compounds and/or industrial use biocides refers to industrial use compositions and/or institutional use products and/or fabric and home care products and/or personal care products defined in more detail in paragraph [3059] of Reference RF1 .
  • the converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3060] of Reference RF1 .
  • the converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3061 ] of Reference RF1 .
  • agrochemical composition typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary.
  • agrochemical compositions typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary.
  • active ingredients and auxiliaries are described in more detail in Reference RF1 , paragraph [4001 ].
  • the agrochemical composition may take the form of any customary formulation.
  • the agrochemical compositions are prepared in a known manner, e.g. described by Mol- let and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005.
  • the converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes.
  • conversion to compounds mentioned in sections “Polymer” and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof” may be performed as described in these sections as well as the respective paragraphs in Reference RF1 .
  • active pharmaceutical ingredients and/or intermediates thereof comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body.
  • Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient.
  • pharmaceutical excipients comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph [5001 ] of Reference RF1 .
  • the converting step(s) to obtain the active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • animal feed additives human food additives, dietary supplements, as used herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate
  • Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph [5002] of Reference RF1 .
  • the converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • aroma chemical and aroma composition as used herein, comprise a volatile organic substance with a molecular weight between 70-250 g/mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine.
  • the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes.
  • Aroma chemicals can be combined with further aroma chemicals to give an aroma composition.
  • Aroma chemicals and aroma compositions are defined in more detail in paragraph [5003] of Reference RF1 .
  • the converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
  • aqueous polymer dispersion comprises aqueous compositions) comprising dispersed polymer(s) and is defined in more detail in the section [6001 ] entitled “aqueous polymer dispersion” of Reference RF1 .
  • the dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s).
  • emulsion polymer comprises polymer(s) made by free- radical emulsion polymerization.
  • Aqueous polyurethane dispersion(s) are defined in more detail in the section [6002] entitled “Polyurethane dispersions” of Reference RF1 .
  • UV-curable polyurethane(s) is/are defined in more detail in the section [6017] of Reference RF1 .
  • Polyurethane - poly(meth)acrylate hybrid polymer(s) is/are defined in more detail in the section [6016] of Reference RF1 .
  • polymeric dispersant comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph [6020] entitled “Polymeric dispersant” of Reference RF1 .
  • the converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is/are defined in more detail in the section [6003] entitled “Emulsion polymerization” of Reference RF1 .
  • the converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is/are defined in more detail in the section [6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section [6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1 .
  • composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section [6004] entitled “Uses of aqueous polymer dispersions”, section [6005] entitled “Binders for architectural and construction coatings” section [6006] entitled “Binders for paper coating” section [6007] entitled “Binders for fiber bonding” section [6008] entitled “Adhesive polymers and adhesive compositions” section [6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions” section [6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions” section [6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them section [6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use” [
  • Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section [6010] entitled “Polyisocyanates” of Reference RF1 .
  • Hyperbranched polyester polyol(s) and its/their uses are defined in more detail in section [601 1 ] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1 .
  • the converting step(s) to obtain the hyperbranched polyester polyols is/are defined in more detail in the section [6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1 .
  • Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section [6013] entitled “Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1 .
  • Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate ⁇ ) for coating with said coating composition(s) are defined in more detail in section [6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1 .
  • 100% curable coating composition(s) is/are defined in more detail in section [6019] of Reference RF1 .
  • Polymeric dispersants) for inorganic binder compositions is/are defined in more detail in section [6020] of Reference RF1 .
  • the inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section [6021 ] of Reference RF1 .
  • the converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section [6020] of Reference RF1 .
  • inorganic binder composition comprising the polymeric dispersant(s), as used herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section [6021 ] of Reference RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”.
  • Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section [6021 ] of Reference RF1 .
  • cosmetic surfactant comprises non-ionic, anionic, cationic, and amphoteric surfactants and is defined in more detail in paragraph [7002] of Reference RF1 .
  • emollient refers to a chemical compound used for protecting, moisturizing, and/or lubricating the skin and is defined in more detail in paragraph [7003] of Reference RF1 .
  • wax comprises pearlizers and opacifiers and is defined in more detail in paragraph [7004] of Reference RF1 .
  • cosmetic polymer comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph [7005] of Reference RF1 .
  • UV filter refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph [7006] of Reference RF1 .
  • composition and/or formulation thereof with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and/or further cosmetic ingredient refers to personal care and/or cosmetic compositions or formulations defined in more detail in paragraph [7007] of Reference RF1 .
  • the converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is/are defined in more detail in paragraph [7008] of Reference RF1 .
  • the target product is selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or
  • cleaning polymer cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyper branched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded
  • the content of the polytetrahydrofuran in the target product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight- % or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and/or wherein the content of the polytetrahydrofuran in target product is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and/or segregation and/or mass balance and/or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.
  • ISCC International
  • the preferably above-mentioned embodiments of the method comprises the step of converting the product of the method, namely polytetrahydrofuran, which can be achieved or obtained by one of the above-mentioned embodiments, to obtain the target product.
  • a typical middle to large sized process for the production of poly-THF (polytetrahydrofuran) via the intermediate product THF and a typical middle to large sized plant arrangement designed for the production of poly-THF via the intermediate product THF respectively have been considered as base for the simulation carried out.
  • the simulation was performed using Aspen software widely known in the state of the art and commonly used in that cases.
  • the input data for the simulation was the following:
  • the combined thermal energy of all four process vapor streams was 7.6 MW (heat supplied to the system).
  • each of the above described four process vapor streams was fed to an evaporator, i.e. four evaporators were present in the simula- tion, and that the evaporators were fed with feed water in order to generate four water steam streams.
  • the COP was calculated according to the following equation:
  • inventive example 2 has been simulated with the same parameters as in inventive example 1 with the exception that the process vapor stream 101 was not considered, i.e. the system I simulation was operating with the three process vapor streams 102, 103 and 104 and three evaporators accordingly.
  • the combined thermal energy of all four process vapor streams was 5.1 MW (heat supplied to the system).
  • the process I plant arrangement according to inventive example 2 results in 10.1 t/h of water steam generated, i.e. the sum of water steam streams generated by the three evaporators.
  • the power demand (work put into the system) for the evaporators was calculated to be 2.4 MW in total which results in a coefficient of performance (COP) of 3.1 , wherein the COP has been calculated as stated above.
  • COP coefficient of performance
  • Fig. 1 A is a schematic diagram of the chemical reaction to form tetrahydrofuran (THF) from 1 ,4-butanediol, which is reacted under catalytic conditions;
  • THF tetrahydrofuran
  • Fig. 1 B is a schematic diagram of the chemical reaction(s) to form poly-THF starting from THF and AczO (acetic anhydride), including a reaction step wherein MeOH (methanol) is used in a transesterification step;
  • Fig. 2A is a schematic diagram of the process stage to form tetrahydrofuran (THF) from 1 ,4-butanediol, including individual process steps.
  • Fig. 2A also represents a schematic example for a first plant sector for the production of THF from 1 ,4-butanediol as starting material, including individual plant units;
  • Fig. 2B is a schematic diagram of the process stage to form poly-THF starting from THF and AczO (acetic anhydride), including individual process steps.
  • Fig. 2B also represents a schematic example for a second plant sector for the production of poly- THF from THF and AczO, including individual plant units;
  • Fig. 3 is a schematic diagram of a process and/or plant arrangement for the production of poly-THF according to the present invention
  • Fig. 4 is a schematic representation of an evaporator for main heat recovery, wherein a process vapor stream is used as heat source to generate a water steam stream from feed water;
  • Fig. 5 is a schematic diagram of an evaporator positioned in a process vapor stream bypass conduit designed for bypassing a main process vapor stream and also pertains to the preferred embodiment of a preheater;
  • Fig. 6 is a schematic diagram of a source of a process vapor stream in the form of a rectification column.
  • Fig. 7 is a schematic diagram of a compressor arrangement.
  • Fig. 1 A shows the reaction pathway to form tetrahydrofuran (THF) from 1 ,4-butane- diol under catalytic conditions.
  • the reaction can be best described as a ring-forming intramolecular condensation and therefore also gives water as side product which needs to be removed, e.g. in distillation steps.
  • Fig. 1 B shows the two-step reaction pathway to form poly-THF from tetrahydrofuran (THF).
  • the reaction pathway includes a first step wherein THF is polymerized under the presence of acetic anhydride (AczO) to form poly-THF Diacetate.
  • the second step can be best described as a transesterification reaction, wherein methanol (MeOH) is reacted with poly-THF Diacetate to form poly-THF and AcOMe (or MeAc) as side product which needs to be removed.
  • Fig. 2A shows the process stage to form tetrahydrofuran (THF) from 1 ,4-butanediol, including individual process steps and shows a schematic example for a first plant sector for the production of THF from 1 ,4-butanediol as starting material, including individual plant units.
  • the specific process steps and plant units include:
  • a purification step/unit to remove further side products and/or residual starting material and to give THF in high purity.
  • a first preferred process vapor stream 101 according to the invention is provided in the azeotropic distillation step/unit.
  • a second referred process vapor stream 102 according to the invention is provided in the purification step/unit.
  • Fig. 2B shows the process stage to form poly-THF starting from THF and AczO (acetic anhydride), including individual process steps and shows a schematic example for a second plant sector for the production of poly-THF starting from THF and AczO, including individual plant units.
  • the specific process steps and plant units include:
  • a third preferred process vapor stream 103 according to the invention is provided in the transesterification step/unit.
  • a fourth referred process vapor stream 104 according to the invention is provided in the methanol removal step/unit.
  • Fig. 3 is a schematic diagram of a process and/or plant arrangement for the production of poly-THF according to the present invention and in detail discloses the parallel arrangement of four evaporators, i.e. a first evaporator 201 , a second evaporator 202, a third evaporator 203 and a fourth evaporator 204.
  • Each of said evaporators is (designed to be) fed with a process vapor stream provided downstream of the process at an inlet of the heat input side (not depicted in Fig. 3).
  • each of the four evaporators is either fed with feed water 401 or bypassed by the feed water 401 by opening or closing the valves 421 , 422, 423 and 424 respectively which are positioned in front of the inlets of the heat output side of the evaporators.
  • the process and/or plant arrangement according to Fig. 3 also comprises a recirculation conduit 410 designed to recirculate the liquid water phase 520 from the water evaporation unit 501 as feed water to the inlets of the heat output sides of the evaporators.
  • Feed water 401 in particular demineralized water, is fed to inlets of the heat output side of the evaporators for the generation of a first water steam stream 301 on an outlet of the heat output side of the first evaporator 201 , a second water steam stream 302 on an outlet of the heat output side of the second evaporator 202, a third water steam stream 303 on an outlet of the heat output side of the third evaporator 203 and a fourth water steam stream 304 on an outlet of the heat output side of the fourth evaporator 204.
  • Said generated water steam streams 301 , 302, 303 and 304 are combined downstream from the heat output sides of the evaporators and fed to the inlet of a water evaporation unit 501 , in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase 520 and a vapor water phase 510.
  • the vapor water phase downstream from the water evaporation unit 501 is compressed in a compressor arrangement 601 into compressed water vapor of a specific pressure and temperature.
  • the compressed water vapor of a specific pressure and temperature is than fed into a vapor grid 602.
  • Fig. 4 is a schematic representation of one of the at least two, preferably three or four, “heat cycles” according to the invention.
  • Said singe “heat cycle” comprises a first evaporator 201 for main heat recovery which is fed by a first process vapor stream 101 (used as heat source) to generate a first water steam stream 301 from feed water 401 .
  • Said schematic concept mutatis mutandis applies for the other “heat cycles” according to the invention.
  • Fig. 5 is a schematic diagram of an evaporator 201 which is fed with feed water 401 and produces a water steam stream 301 and which is positioned in a process vapor stream bypass conduit 701 designed for bypassing a main process vapor stream conduit 720. Accordingly, the evaporator 201 is either fed with the process vapor stream 101 or bypassed by the process vapor stream 101 by opening or closing control valves 71 1 and 721 positioned in front of the inlet of the heat input side of the evaporator in the process vapor stream bypass conduit (valve 71 1 ) and in the main process vapor stream conduit (valve 721 ).
  • evaporator 201 can either be put into operation or can be left out of the system/process.
  • the process vapor stream 101 is usually cooled down in an air cooler 901 .
  • Fig. 5 also shows the concept of an optional preheater 801 wherein feed water 401 is preheated before the feed water 401 is fed to the inlet of the heat output side of the evaporator 201 and wherein the preheater utilizes the remaining thermal energy (heat) of the process vapor stream exiting the evaporator 201 as heating medium.
  • Fig. 6 shows a preferred source 1 1 1 of a process vapor stream 101 according to the invention in the form of a rectification column or fractionating column.
  • the process vapor stream 101 is fed to the heat input side of an evaporator 201 which is fed with feed water 401 and generates a water steam stream 301 .
  • Said source 1 1 1 may be associated with any of the process steps/units according to the present invention.
  • said source 1 1 1 1 of a process vapor stream 101 in the form of a rectification column or fractionating column is associated with one of the following process steps/units:
  • the source 1 1 1 preferably provides a process vapor stream 101 with the following set of parameters:
  • - a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara.
  • At least two, preferably two, more preferably four of the process vapor streams according to the invention derive from a source in the form of a rectification column or fractionating column.
  • Fig. 7 is a schematic diagram of a compressor arrangement 601 .
  • compressor stages are arranged in the form of a compressor cascade of a first, a second and a third compressor C1 , C2, C3, namely as part of a first, a second and a third compressor unit 61 1 , 612, 613.
  • a modelling of the compressor arrangement 601 is shown with the water evaporation unit 501 , which generates a vapor water phase to be fed into the compressor arrangement 601 and a vapor grid 602 which is fed by the compressed water vapor of a specific pressure and temperature as provided by the compressor arrangement 601 .
  • the compressor arrangement 601 is provided with a first compressor unit 61 1 , a second compressor unit 612 and a third compressor unit 613, i.e. a “compressor cascade”.
  • the individual compressor units 61 1 , 612 and 613 preferably comprise a steam compressor C1 , C2 and C3 each of all in the form of either a screw compressor or alternatively a radial fan or alternatively an axial turbo compressor.
  • each of the compressor units 61 1 , 612 and 613 respectively combines a first, a second and a third spray nozzle S1 , S2 and S3 with the first, the second and the third compressor C1 , C2 and C3 to respectively provide a compressor unit 61 1 , 612 and 613 as mentioned above for spraying off the live steam.
  • Respective feed water is provided by way of a first, a second and a third pump P1 , P2 and P3 to a respective spray nozzle S1 , S2 and S3.

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Abstract

Process for the production of polytetrahydrofuran (poly-THF), wherein - associated with one, two or more process stages of the process of producing polytetrahydrofuran (poly-THF) at least two process vapor streams are provided downstream of the process, and - a first process vapor stream is fed to an inlet of the heat input side of a first evaporator of at least two evaporators, and - a second process vapor stream is fed to an inlet of the heat input side of a second evaporator of at least two evaporators, and - the first process vapor stream and the second process vapor stream are further used or recirculated in the process from outlets of the heat input side of the first evaporator and the second evaporator.

Description

Process and plant arrangement for the production of polytetrahydrofuran (poly-THF)
FIELD OF THE INVENTION
The present invention relates to a process and plant arrangement for the production of polytetrahydrofuran (poly-THF). The invention is defined in the claims as attached.
BACKGROUND OF THE INVENTION Polytetrahydrofuran (poly-THF) is a polymer consisting of the monomeric unit [O- CH2-CH2-CH2-CH2] and can be described with the chemical formula HO-((CH2)4O)nH. Accordingly, poly-THF is a mixture of polyether diols terminated with alcohol groups. Poly-THF is widely used as a starting material for making elastic fibres, polyurethane resins, thermoplastic polyurethane, thermoplastic polyesters, polyetheramide and cast polyurethane elastomers, used for instance in the wheels of roller skates and skateboards.
The process for the production of poly-THF (polytetrahydrofuran) via the intermediate tetrahydrofuran (THF) is long established and well known, cf. for example WO 96/23833 A1 . The process involves several chemical reactions and other reaction steps such as purifications.
Generally, the overall process for the production of poly-THF starts from 1 ,4-butane- diol, which is reacted under catalytic conditions to form tetrahydrofuran (THF) and water. Water is usually distilled off in one or more distillation steps, in particular by azeotropic and/or pressure distillation. The THF obtained from said reaction is usually purified in one or more purification steps known in the state of the art.
The obtained and optionally purified intermediate compound THF is than used as starting material in a polymerization reaction to form poly-THF. One of the main reaction routes relies on a reaction of THF with acetic anhydride (AczO), followed by a step in which residual THF is removed, by a reaction step wherein MeOH (methanol) is used in a transesterification and a step wherein residual MeOH is removed.
The chemical reaction(s) and conditions for the production of the intermediate THF is for example disclosed in “Ullmann, 2023 - Tetrahydrofuran”, US 7,098,349 B2 and DE 3432575 C2 (THF synthesis).
The chemical reaction(s) and conditions for the production of poly-THF from THF is for example disclosed in DE 10 2006 009 150 B4 and WO 96/23833. A1 .
Up to today existing plants or plant arrangements for the industrial production of poly- THF (and THF) do not sufficiently utilize the process heat deriving from process vapor streams originating from the chemical reaction steps, purification steps and other steps of the overall process. On the contrary, most of the existing plants operate with air coolers, accordingly thermal energy (heat) of process vapor streams is lost or even worse additional energy generated with fossil fuels is needed to cool down process vapor streams.
At the same time chemical production sites (e.g. Ludwigshafen, BASF) rely on heating grids with water steam as energy carrier for supplying thermal energy which is needed for chemical reactions and the like. Said heating grids are currently mainly heated with fossil fuels.
The unused thermal energy (heat) in the current production processes and plant arrangements for the production of poly-THF and the additional demand of fossil fuels, which are needed to cool down process vapor streams and/or to heat the heating grids of the chemical production sites causes the emission of greenhouse gases. This is a serious problem in times of global warming.
Additionally, current processes for the production of poly-THF and the respective plant arrangements for the production of poly-THF are unstable due to the usage of air cooler whose operation can get crucial at high ambient temperature. This limited cooling capacity is a bottleneck during summertime and often leads to an unwanted shot-down of the production process I plant arrangement or to lowering the production capacity.
Moreover, a technical problem arises since many of the process vapor streams generated in the process for the production of poly-THF are considered as too less energy efficient for recovering their thermal energy. When taken alone the single process vapor streams have a relatively i) low temperature, ii) low mass flow and iii) low thermal energy.
Accordingly, there is a demand in industry for an improved process and plant arrangement for the production of poly-THF, wherein preferably the emission of greenhouse gases is reduced and wherein unwanted shot-downs of the production process I plant arrangement or lowering the production capacity at high ambient temperature, especially during summer time are obsolete.
Further, in order to improve the CO2 balance, it has been proven to be increasingly important to generate green steam, i.e. water vapor mostly generated by electricity from regenerative electrical energy sources like wind, solar or the like and by using waste heat from chemical production processes. Even if a variety of methods for using waste heat from chemical production processes for energy recovery are generally known, this must regularly be questioned in terms of efficiency, technical effort, feasibility and/or a realistic possibility of integration into existing processes, systems and plant arrangements such as the one mentioned at the beginning.
This is particularly questionable if heat transfer media with a low heat content are provided which only appear to be usable for releasing waste heat into the environment. The use of heat pumps in the chemical industry is well known in this regard. With the current energy crisis and the growing pressure for decarbonization, they are also becoming an increasingly attractive option for the (large-scale) process industry. A heat pump uses existing heat from a heat transfer media I heat source at a low temperature level and brings it to a higher temperature level using electricity and a refrigerant or the like workingfluid. Accordingly, a suitable heat source is the basic requirement for using a heat pump. In principle, different concepts come into consideration for this. However, there are restrictions to be accounted for in large- scale chemical processes. In principle, heat sources to be considered are: (waste) air or (waste) water, the ground, refrigeration systems or cooling systems, combined heat of power plants or from compressed air generation and, in this case, waste heat from production processes. In principle, temperatures of just a few degrees plus are sufficient, so that previously unused waste heat can in principle be made usable with a heat pump.
However, the aim should at least be to enable the steam level that can be achieved with a heat pump to be used in e.g. chemical processes and a certain efficiency should also be given. The efficiency is in most cases, also here, determined via the COP value (“Coefficient of Performance” - in German also known as “Leistung- szahl”) as a measure of the efficiency of a heat pump. The higher the COP value, the more efficiently the heat pump works. In general, good COP values are between 3 and 5. A COP below 3 usually indicates that a heat pump can only work sub optimally. The COP is determined under laboratory conditions and only relates to the heat pump, not to the peripherals. However, which COP value is considered good varies depending on the specific application and the type of heat pump. In some cases lower COP are thus also acceptable.
As described in the article “Use of heat pumps in the chemical industry” by Harald Roth (November 8, 2022) in Chemistry & Technology under Energy & Utilities (https://www.chemietechnik.de/energie-utilities/einsatz-von-waermepumpen-in-der- chemischen-industrie-788.html#:~:text=Doch%20auch%20die%20tech- nisch%20ausgereiften,Trocknungs%2D%20Destilla- tions%2D%20oder%20Heizprozesse) depending on the heat source, classic heat pumps achieve a temperature level of up to 60 °C, while high-temperature heat pumps (HT) reach up to 160 °C. I It will still be some time before such systems are commercially available - in this respect, the results subsequently realized and for large-scale industrial use are outstanding and extremely far-reaching.
It is generally known that - in the event that the required temperature cannot be achieved with one heat pump alone - several heat pumps can also be combined in a cascade connection. Not only can the temperature level be increased, but the individual devices can also be switched on and off as needed. This means that in some cases this is a better option than using a single large heat pump.
On the other hand, technically sophisticated models can already be used in many areas in the chemical industry, such as for plastic production and processing at temperatures between 80 and 140 °C, for generating process steam and for drying, distillation or heating processes. Sometimes it also makes sense to use a heat pump only for preheating and thus reduce the use of fossil fuels. However, such concepts can still be improved; to date, most concepts are only suitable for generating heating power via steam at very low pressure levels of up to 2 bar. A large part of the steam is used as process steam in production, for example for drying products, heating reactors or for distillation.
SUMMARY OF THE INVENTION
It was a primary object of the present invention to provide for such an improved process and plant arrangement for the production of polytetrahydrofuran (poly-THF). Furthermore, the improved process and plant arrangement for the production of poly- THF should preferably be easily integrated into existing processes and plant arrangements and should also be economically attractive.
The present invention concerns in its categories a process for the production of poly- THF and a plant arrangement designed for the production of poly-THF. Embodiments, aspects or features disclosed for or in connection with one of these categories in each case analogously apply for the other categories of the invention.
If not stated otherwise, preferred embodiments, aspects or features of the present invention can be combined with other embodiments, aspects or features, especially with other preferred embodiments, aspects or features, irrespectively of the categories to which the embodiments, aspects or features relate. The combination of preferred embodiments, aspects or features with other preferred embodiments, aspects or features in each case again results in preferred embodiments, aspects or features.
In accordance with the primary object of the invention as stated above, the present invention relates to a process for the production of polytetrahydrofuran (poly-THF), wherein
- associated with one, two or more process stages of the process of producing polytetrahydrofuran (poly-THF) at least two process vapor streams are provided downstream of the process, and
- a first process vapor stream is fed to an inlet of the heat input side of a first evaporator of at least two evaporators, and
- a second process vapor stream is fed to an inlet of the heat input side of a second evaporator of at least two evaporators, and - the first process vapor stream and the second process vapor stream are further used or recirculated in the process from outlets of the heat input side of the first evaporator and the second evaporator, and
- feed water, in particular demineralized water, is fed to inlets of the heat output side of the first evaporator and the second evaporator for the generation of a first water steam stream on an outlet of the heat output side of the first evaporator and a second water steam on an outlet of the heat output side of the second evaporator, and
- the generated first water steam stream and the generated second water steam stream downstream from the heat output sides of the first evaporator and the second evaporator are combined and fed to the inlet of a water evaporation unit, in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase, and
- the vapor water phase downstream from the water evaporation unit is com-pressed in a compressor arrangement into compressed water vapor of a specific pressure and temperature, in particular is compressed by using electrical energy from a renewable energy source, and
- the compressed water vapor of a specific pressure and temperature is fed into a vapor grid, in particular a heating network.
Herein, and throughout the present text, the term “process vapor stream” designates a vapor stream deriving from a process stage of the production of poly-THF. Said process stage can be of any kind and may for example be a reaction process, a purification process, a distillation process or a removal process. The process vapor streams according to the present invention are not limited to a certain chemical composition of the vapor and may comprise, starting materials, intermediates, added compounds and/or reaction products in any given ratio.
Herein, and throughout the present text, the term “evaporator” generally can be any kind of “heat exchanger”. The evaporator is generally part of a heat pump cycle wherein the evaporated steam is provided for further use, in particular further use in an industrial steam grid.
Herein, and throughout the present text, certain aspects and features such as process stages, process vapor streams, evaporators, generated water steam streams and the like are present in plural and thus labelled with terms such as “more than one” or “at least two”. This means that at least a first embodiment and a second embodiment of said aspect or feature are present within the process or plant arrangement according to the invention, wherein the individual embodiments are independent from each other and can either be structurally identical, e.g. size and type of the first, the second and the optionally present third and fourth evaporators may be the same, or structurally different, e.g. the origin and chemical composition of the first process vapor stream and the second process vapor stream may differ substantially.
The main concept of the present invention lies within the parallel utilization of thermal energy from each of the at least two process vapor streams. Within the process of the present invention the thermal energy of every individual process vapor stream, designated as first, second, third, fourth etc. process vapor stream, is transferred to feed water in order to generate a water steam stream, designated as first, second, third, fourth etc. water steam stream. Said transfer of thermal energy is conducted in individual evaporators, designated as first, second, third, fourth etc. evaporator. E.g., in a process according to the present invention a first process vapor stream is used as heat source to generate a first water steam stream, wherein said heat transfer is conducted in a first evaporator; in parallel a second process vapor stream is used as heat source to generate a second water steam stream, wherein said heat transfer is conducted in a second evaporator and so on.
Accordingly, the inventive concept identifies at least two process vapor streams provided downstream of the process which are suitable as heat source for heat exchangers in the form of at least two evaporators.
The invention utilizes the combined thermal energy of the least two process vapor streams which when taken alone might not contain enough thermal energy. Thus, a relevant part of the process heat from the process vapor streams associated with the production of poly-THF is transferred to compressed water vapor of a specific pressure and temperature which is fed to a vapor grid, in particular a heating network, instead of being “wasted”. Since heating networks of chemical production sites are currently mainly heated with fossil fuels, the process according to the invention improves energy efficiency and reduces emissions of greenhouse gases. Emissions of greenhouse gases are further reduced by preferably using electrical energy from a renewable energy source to run the compressor arrangement.
The implementation and utilization of the at least two evaporators according to the invention instead of air coolers also solves the problem of limited cooling capacity which is a bottleneck at high ambient temperature during summertime. Furthermore only a single compressor arrangement is needed to compress the combined water steam streams generated by the at least two or more evaporators which minimizes investment costs and space usage.
Advantageous developments of the invention are hereinafter found and described in accordance with the dependent claims and indicate in detail advantageous options and developments, which can be realized within the concept of the invention described above and within the scope of the object of the invention as well as with regard to further advantages. In the following, preferred developments of the process and plant arrangement will be described.
Preferred is a process of the present invention wherein at least three process vapor streams are provided downstream of the process and wherein
- a third process vapor stream is fed to an inlet of the heat input side of a third evaporator, and
- the third process vapor stream is further used or recirculated in the process from an outlet of the heat input side of the third evaporator, and
- feed water, in particular demineralized water, is fed to an inlet of the heat output side of the third evaporator for the generation of a third water steam stream on an outlet of the heat output side of the third evaporator, and
- the generated third water steam stream downstream from the heat output side of the third evaporator is combined with the generated first and second water steam stream downstream from the heat output sides of the first and second evaporator and fed to the inlet of the water evaporation unit, in particular flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase.
According to this preferred embodiment a total number of at least three process vapor streams associated with at least three process stages of the process of producing poly-THF are provided in parallel and the combined thermal energy of said at least three process vapor streams is utilized instead of being “wasted”. This makes the process even more efficient and reduces the emission of greenhouse gases even more.
More preferred is a process of the present invention wherein at least four process vapor streams are provided downstream of the process and wherein - a fourth process vapor stream is fed to an inlet of the heat input side of a fourth evaporator, and
- the fourth process vapor stream is further used or recirculated in the process from an outlet of the heat input side of the fourth evaporator, and
- feed water, in particular demineralized water, is fed to an inlet of the heat output side of the fourth evaporator for the generation of a fourth water steam stream on an outlet of the heat output side of the fourth evaporator, and
- the generated fourth water steam stream downstream from the heat output side of the fourth evaporator is combined with the generated first, second and third water steam stream downstream from the heat output sides of the first, second and third evaporator and fed to the inlet of the water evaporation unit, in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase.
According to this more preferred embodiment of the present invention a total number of at least four process vapor streams associated with at least four process stages of the process of producing poly-THF are provided in parallel and the combined thermal energy of said at least four process vapor streams is utilized instead of being “wasted”. This makes the process even more efficient and reduces the emission of greenhouse gases even more.
Preferred is a process according to the invention, wherein the liquid water phase from the water evaporation unit is further used or recirculated. Said preferred process reduces water waste and makes the process even more feasible and sustainable. More preferably the liquid water phase from the water evaporation unit is recirculated as feed water, which is fed to the inlets of the heat output side of the evaporators.
Preferred is a process according to the present invention, wherein at least one, preferably all, of the two or more, preferably four, process vapor streams provided downstream of the process derive from the following process steps and process stages:
- distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol,
- purification step in the process stage of producing THF from 1 ,4-butanediol, - transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AC2O),
- methanol removal step in the process stage of producing poly-THF from THF and AczO.
This means that the process vapor streams provided in the process of the present invention are associated with specific individual process steps and process stages, wherein said process steps and process stages are part of the overall process of producing poly-THF. Accordingly, the inventive concept is applicable to a number of different sources of process vapor streams which makes it feasible and economically attractive.
Even more preferred is a process according to the present invention, wherein four process vapor streams are provided downstream of the process and wherein
- the first process vapor stream of the four process vapor streams derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
- the second process vapor stream of the four process vapor streams derives from purification step in the process stage of producing THF from 1 ,4-butanediol, and
- the third process vapor stream of the four process vapor streams derives from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO), and
- the fourth process vapor stream of the four process vapor streams derives from a methanol removal step in the process stage of producing poly-THF from THF and AC2O.
Said more preferred embodiment utilizes a total number of four process vapor streams, wherein each of the four individual process vapor streams is associated with one out of four process steps and process stages of the process of producing poly-THF. The combined thermal energy of said four individual process vapor streams as specified above is used as heat source for the generation of four individual water steam streams, wherein the heat transfer is conducted in four individual evaporators. Accordingly, four process vapor streams are provided in parallel and the combined thermal energy of said four process vapor streams as specified above is utilized instead of being “wasted”. This makes the process even more efficient and reduces the emission of greenhouse gases even more. It is a special achievement of the present invention to identify particularly suitable sources of process vapor streams out of the numerous options for different process steps in the process of producing poly-THF.
Preferred is a process according to the present invention, wherein the temperature of each of the at least two, preferably four, process vapor streams provided downstream of the process is at least 50 °C, preferably is at least 55 °C.
According to this preferred embodiment, each of the process vapor streams which are utilized as heat source have a minimum temperature of at least 50 °C, preferably of at least 55 °C. This leads to a particularly efficient and economically beneficial mode of operation of the process according to the present invention since said defined minimum temperature ensures a certain amount of thermal energy of the at least two, preferably four, process vapor streams for the generation of the at least two, preferably four, water steam streams in the evaporators. Again, this takes into account that the thermal energy of at least two process vapor streams is utilized in parallel, i.e. thermal energy is combined, in preferred cases the thermal energy of three, four or more process vapor streams is utilized in parallel.
Preferred is a process according to the present invention, wherein the temperature of each of the at least two, preferably four, process vapor streams provided downstream of the process is in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C.
More preferably four process vapor streams are provided downstream of the process, each of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and wherein
- the first process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
- the second process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, derives from purification step in the process stage of producing THF from 1 ,4- butanediol, and - the third process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, derives from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO), and
- the fourth process vapor stream of the four process vapor streams having a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, derives from a methanol removal step in the process stage of producing poly- THF from THF and acetic anhydride (AczO).
Accordingly, the inventive concept identifies suitable sources of process vapor streams which are similar in temperature. Those suitable sources of process vapor streams which are similar in temperature are more preferably associated with specific individual process steps and process stages as identified above, wherein said process steps and process stages are part of the overall process of producing poly- THF.
The utilization of process vapor streams which are similar in temperature allows for a particularly facile and effective process wherein the synergistic effect of process vapors condensing at approximately same temperatures are utilized. The mode of operation and/or the design of plant elements such as pipes, valves, evaporators and the like can thus be kept simple which reduces investment and operational costs and makes the implementation of the process according to the present invention into existing processes and plant arrangements feasible.
Preferred is a process according to the present invention, wherein the pressure of each of the at least two, preferably four, process vapor streams provided downstream of the process is in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara.
More preferred is a process according to the present invention, wherein pressure and temperature of the at least two, preferably four, process vapor streams provided downstream of the process are in the ranges as defined above.
Even more preferred is a process according to the present invention, wherein pressure and temperature of the at least two, preferably four, process vapor streams provided downstream of the process are in the ranges as defined above and wherein the two or more, preferably four, process vapor streams provided downstream of the process derive from the process steps and process stages as defined above.
A particularly preferred process according to the present invention provides and utilizes the following four process vapor streams:
- a first process vapor stream, wherein said first process vapor stream
- derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
- has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
- has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara, and
- a second process vapor stream, wherein said second process vapor stream
- derives from a purification step in the process stage of producing THF from 1 ,4-butanediol, and
- has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
- has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara, and
- a third process vapor stream, wherein said third process vapor stream
- derives from a transesterification step in the process stage of producing poly- THF from THF and acetic anhydride (AczO), and - has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
- has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara, and
- a fourth process vapor stream, wherein said fourth process vapor stream
- derives from a methanol removal step in the process stage of producing poly- THF from THF and acetic anhydride (AczO), and
- has a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C, and
- has a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara.
Preferred is a process according to the present invention, wherein the total amount of thermal energy of process vapor streams deriving from a process step in the process stage of producing THF (tetrahydrofuran) is at least 1 .5 MW per production of 1 kg THF, preferably is at least 2 MW per production of 1 kg THF.
More preferably, the process according to the present invention provides and utilizes a first process vapor stream deriving from a distillation step, preferably an azeotropic distillation, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butane- diol and a second process vapor stream deriving from a purification step in the process stage of producing THF from 1 ,4-butanediol, wherein the total amount of thermal energy of the combined first and second process vapor stream is at least 1 .5 MW per production of 1 kg THF, preferably is at least 2 MW per production of 1 kg THF.
Also preferred is a process according to the present invention, wherein the total amount of thermal energy of process vapor streams deriving from a process step in the process stage of producing poly-THF is at least 1 .5 MW per production of 1 kg poly-THF, preferably is at least 2 MW per production of 1 kg poly-THF. More preferably, the process according to the present invention provides and utilizes a third process vapor stream deriving from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO) and a fourth process vapor stream deriving from a methanol removal step in the process stage of producing poly-THF from THF and acetic anhydride (AczO), wherein the total amount of thermal energy of the combined third and fourth process vapor stream is at least 1 .5 MW per production of 1 kg poly-THF, preferably is at least 2 MW per production of 1 kg poly-THF.
In some cases it might be beneficial that the process according to the present invention is characterized in that the combined mass flow of the at least two, preferably four, process vapor streams provided downstream of the process is at least 40 t/h, preferably is at least 50 t/h, more preferably is at least 60 t/h.
In some cases it might be beneficial that the process according to the present invention is characterized in that the total amount of water steam generated by the at least two, preferably four, evaporators is at least 8 t/h, preferably is at least 10 t/h, more preferably is at least 12 t/h.
Preferred is a process according to the present invention, wherein at least one, preferably all, of the at least two, preferably four, evaporators are positioned in individual process vapor stream bypass conduits designed for bypassing a main process vapor stream conduit and are either fed with the process vapor stream or are bypassed by the process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the evaporators in the process vapor stream bypass conduits and in the main process vapor stream conduits.
According to this preferred embodiment of the present invention and assuming the presence of four evaporators for heat transfer from four process vapor streams to feed water in order to generate four water steam streams as the preferred mode of operation the process involves:
- a first evaporator positioned in a first process vapor stream bypass conduit designed for bypassing a first main process vapor stream conduit, wherein the first evaporator is either fed with the first process vapor stream or is bypassed by the first process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the first evaporator in the first process vapor stream bypass conduit and in the first main process vapor stream conduit, and - a second evaporator positioned in a second process vapor stream bypass conduit designed for bypassing a second main process vapor stream conduit, wherein the second evaporator is either fed with the second process vapor stream or is bypassed by the second process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the second evaporator in the second process vapor stream bypass conduit and in the second main process vapor stream conduit, and
- a third evaporator positioned in a third process vapor stream bypass conduit designed for bypassing a third main process vapor stream conduit, wherein the third evaporator is either fed with the third process vapor stream or is bypassed by the third process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the third evaporator in the third process vapor stream bypass conduit and in the third main process vapor stream conduit, and
- a fourth evaporator positioned in a fourth process vapor stream bypass conduit designed for bypassing a fourth main process vapor stream conduit, wherein the fourth evaporator is either fed with the fourth process vapor stream or is bypassed by the fourth process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the fourth evaporator in the fourth process vapor stream bypass conduit and in the fourth main process vapor stream conduit.
Said preferred embodiment involving individual process vapor stream bypass conduits as described above allows for a certain flexibility of the process as individual evaporators are either in operation, i.e. are fed with a process vapor stream, or are not in operation, i.e. are bypassed by a process vapor stream. Accordingly, the process can react to fluctuating conditions during the process of producing poly-THF, e.g. if certain process stages or process steps are out of operation due to maintenance work or when the production capacity of the plant arrangement for the production of poly-THF or certain parts or units of the plant arrangement for the production of poly-THF is reduced. E.g., a process usually operating with four evaporators in parallel might also operate with only three or two of the evaporators.
Preferred is a process according to the present invention, wherein one, more than one or all of the at least two, preferably four, evaporators are either fed with the feed water or are bypassed by the feed water by opening or closing a valve positioned in front of the inlets of the heat output side of the evaporators. According to this preferred embodiment of the present invention and assuming the presence of four evaporators for heat transfer from four process vapor streams to feed water in order to generate four water steam streams as the preferred mode of operation the process involves:
- a first evaporator, which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the first evaporator, and
- a second evaporator, which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the second evaporator, and
- a third evaporator, which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the third evaporator, and
- a fourth evaporator, which is either fed with the feed water or is bypassed by the feed water by opening or closing a valve positioned in front of the inlet of the heat output side of the fourth evaporator.
Said preferred embodiment involving individual valves positioned in front of the inlets of the heat output side of the evaporators as described above allows for a certain flexibility of the process as individual evaporators are either fed with feed water or are bypassed by the feed water. Accordingly, the process can react to fluctuating conditions during the process of producing poly-THF, e.g. if certain process stages or process steps are out of operation due to maintenance work or when the production capacity of the plant arrangement for the production of poly-THF or certain parts or units of the plant arrangement for the production of poly-THF is reduced. Furthermore this allows for individual maintenance of individual evaporators without interrupting the overall process. E.g., a process usually operating with four evaporators in parallel might also operate with only three or two of the evaporators.
Preferred is a process according to the present invention, wherein the at least two, preferably four, process vapor streams provided in the process are associated with process stage units of the process of producing THF and/or poly-THF within the same plant or plant arrangement, more preferably the process stage units have a maximum distance of 100 m to each other. More preferred is a process according to the present invention, wherein four process vapor streams are provided from process stage units within the same plant or plant arrangement having a maximum distance of 100 m to each other, wherein
- the first process vapor stream provided derives from a distillation process stage unit, preferably an azeotropic distillation process stage unit, in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol, and
- the second process vapor stream provided derives from a purification process stage unit in the process stage of producing THF from 1 ,4-butanediol, and
- the third process vapor stream provided derives from a transesterification process stage unit in the process stage of producing poly-THF from THF and acetic anhydride (AczO), and
- the fourth process vapor stream provided derives from a methanol removal process stage unit in the process stage of producing poly-THF from THF and acetic anhydride (AC2O).
Accordingly, it is preferred that the process vapor streams provided in the process are associated with process stage units of the process of producing THF and/or poly- THF are in close proximity to each other, thus allowing for a cost effective and facile installation and implementation of the system I process according to the present invention. Said preferred arrangement makes the parallel utilization of two, three, four or more heat sources in the form of process vapor streams feasible, minimizes loss of thermal energy in transport processes and inter alias saves piping material.
Preferred is a process according to the present invention, wherein the vapor water phase downstream from the water evaporation unit, in particular flash drum, is compressed in a compressor arrangement into compressed water vapor with a pressure and temperature in the range of from
- 2.5 bara to 3.0 bara and 127 °C to 200 °C, or
- 5.0 bara to 6.8 bara and 151 °C to 200 °C, or
- 12 bara to 14 bara and 187 °C to 250 °C, or
- 16 bara to 18.8 bar and 201 °C to 250 °C. Above described parameter sets of pressure and temperature ranges of the vapor water phase downstream from the water evaporation unit are in particular suitable for feeding the vapor water phase into a vapor grid, in particular a heating network.
Preferred is a process according to the present invention, wherein the feed water is preheated in one, two or more preheaters before the feed water is fed to the inlets of the heat output side of one, two or more of the at least two evaporators and wherein the one, two or more preheaters utilize one, two or more of the at least two process vapor streams exiting the at least two evaporators as heating medium.
Preferred is a process according to the present invention, wherein the feed water is preheated before the feed water is fed to the inlets of the heat output side of the evaporators in
- a first preheater before the feed water is fed to the inlet of the heat output side of a first evaporator wherein the first preheater utilizes a first process vapor stream exiting the first evaporator as heating medium, and/or, preferably “and”
- a second preheater before the feed water is fed to the inlet of the heat output side of a second evaporator wherein the second preheater utilizes a second process vapor stream exiting the second evaporator as heating medium, and/or, preferably “and”
- a third preheater before the feed water is fed to the inlet of the heat output side of a third evaporator wherein the third preheater utilizes a third process vapor stream exiting the third evaporator as heating medium, and/or, preferably “and”
- a fourth preheater before the feed water is fed to the inlet of the heat output side of a fourth evaporator wherein the fourth preheater utilizes a fourth process vapor stream exiting the fourth evaporator as heating medium.
According to this preferred embodiment of the present invention the remaining thermal energy of the process vapor streams existing the evaporators is utilized, thus making the overall process even more efficient and reducing greenhouse emissions even further. In accordance with the primary object of the invention as stated above, the present invention relates to a plant arrangement designed for the production of poly-THF, comprising
- a first plant sector for the production of THF from 1 ,4-butanediol as starting material, and
- a second plant sector for the production of poly-THF from THF and AczO, and
- at least two separate sources of process vapor streams in the first and/or second plant sector, and
- at least two evaporators in the first and/or second plant sector which are designed
- to be fed by a process vapor stream from one of at least two separate sources of process vapor streams in the first and/or second plant sector at the inlet of a heat input side, and
- to be fed by feed water at the inlet of a heat output side, and
- to eject a water steam stream at the outlet of the heat output side, and
- a water evaporation unit, in particular a flash drum, downstream from the heat output sides of the at least two evaporators which is designed
- to be fed by the combined water steam streams from the outlets of the at least two evaporators, and
- to form a liquid water phase and a vapor water phase by flash evaporation of the combined water steam streams, and - to eject the vapor water phase obtained from the flash evaporation, and
- a compressor arrangement downstream from the water evaporation unit designed
- to be fed with the vapor water phase from the water evaporation unit, and
- to compress the vapor water phase to a specific pressure and temperature, and
- to feed the compressed vapor water phase into a vapor grid, in particular a heating network.
Herein, and throughout the present text, the term “plant arrangement” designates a chemical production site which comprises several individual plant units and which can be subdivided in two or more plant sectors. The plant sectors are distinguished with regard to their target product, i.e. a first plant sector produces THF and a second plant sector produces poly-THF. Usually and preferably the individual plant units and sectors of said plant arrangement are in close proximity to each other, more preferably all parts of the plant arrangement are within the same building.
Herein, and throughout the present text, the term “water evaporation unit” designates a construction or process or plant unit or the like feature capable of performing evaporation -full evaporation or partial evaporation- to a water steam, preferably at least in part by flash evaporation, in order to produce a vapor water phase and a liquid water phase by means of a partial evaporation, possibly only a liquid water phase by means of a full evaporation. Flash evaporation occurs when a water steam stream undergoes a reduction in pressure by passing through a throttling valve or other throttling device. It is particularly preferred that the water evaporation unit is a flash drum wherein a throttling valve or device is located at the entry into a pressure vessel so that the flash evaporation occurs within the vessel.
Herein, and throughout the present text, the term “compressor arrangement” designates a construction/process/plant unit capable of compressing a vapor phase to a certain pressure and temperature level. Said compressor arrangement may consist of a single compressor or may comprise two or more compressors each in a compressor stage of the compressor arrangement, respectively a compressor unit or units.
Compressor stages may preferably be arranged in the form of a compressor cascade of compressors or compressor units, e.g. three compressors or compressor units in a row as shown in an embodiment of Fig. 7.
For providing a compressor unit a compressor may preferably be combined with another element such as a valve, a spray nozzle or the like element supporting compressing of the vapor phase to a certain pressure and temperature level; said element may be arranged as an intermediate element between a first and a second compressor of a compressor arrangement.
An individual compressor preferably is a steam compressor of specific kind, namely in the form of a screw compressor, a radial fan or an axial turbo compressor. A combination of different kinds of compressors is possible in said compressor arrangement. More preferably all compressors in said compressor arrangement are steam compressors of the same kind, namely either in the form of a screw compressor or alternatively a radial fan or alternatively an axial turbo compressor.
Further compressor blades are sensitive to water droplets. In particular -with the order of a screw compressor, a centrifugal fan, an axial turbo compressor- the compressor blades become increasingly sensitive to water droplets. In particular the blades of an axial turbo compressor should not extensively be exposed to water droplets. An isolated solution can be provided for a screw compressor or a centrifugal fan to provide that water is sprayed in for cooling. Preferably it is of advantage that the live steam is sprayed off in at least one compressor stage of the compressor arrangement, in particular by spraying water in at least one compressor stage, preferably all compressor stages. At least and in particular the first compressor stage of said compressor arrangement, in particular where in a compressor cascade, combines a spray nozzle with the compressor to respectively provide a compressor unit as mentioned above for spraying off the live steam.
Water is usually added to spray off the live steam after the compressor with the longest possible inlet section. Ideally, the water is sprayed to support or even accelerate evaporation and to avoid the formation of droplet streaks. Preferably all compressor stages each combines a spray nozzle with the compressor to provide a compressor unit. Preferably water should be sprayed in after each compressor stage to regulate the temperature (and to increase the steam yield). However, this can also be done before sensitive blades. Therein preferably it is observed that the inlet distance in the superheated steam is sufficient and droplets have evaporated by the time they reach the blades.
Preferably at least one or some, preferably all of the compressor stages are driven with electrical power from regenerative energy sources.
Thus, in a preferred embodiment, all power consumptions explained above is generated green, i.e. the power is generated from regenerative electrical energy sources like wind, solar or the like “green” energy sources.
Preferred is a plant arrangement according to the present invention, comprising
- a first source of a first process vapor stream in the first plant sector, and
- a second source of a second process vapor stream in the first plant sector, and
- a third source of a third process vapor stream in the second plant sector, and
- a fourth source of a fourth process vapor stream in the second plant sector, and
- a first evaporator in the first plant sector designed to be fed by the first process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a first water steam stream at the outlet of the heat output side, and
- a second evaporator in the first plant sector designed to be fed by the second process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a second water steam stream at the outlet of the heat output side, and
- a third evaporator in the second plant sector designed to be fed by the third process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a third water steam stream at the outlet of the heat output side, and
- a fourth evaporator in the second plant sector designed to be fed by the fourth process vapor stream at the inlet of a heat input side and designed to be fed by feed water at the inlet of a heat output side and designed to eject a fourth water steam stream at the outlet of the heat output side, and
- a water evaporation unit, in particular a flash drum, downstream from the heat output sides of the first, second, third and fourth evaporator which is designed to be fed by the combined first, second, third and fourth water steam streams from the outlets of the first, second, third and fourth evaporator.
Preferably one, two or more, preferably all, of the at least two, preferably four, separate sources of process vapor streams in the first and/or second plant sector are reactors or columns, preferably rectification columns.
Preferred is a plant arrangement according to the present invention, wherein at least one, preferably all, of the at least two, preferably four, separate sources of process vapor streams are selected from the following process stage units
- a distillation unit in the first plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material,
- a purification unit in the first plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material,
- a transesterification unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO,
- a methanol removal unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO.
More preferably the plant arrangement according to the present invention, comprises four separate sources of process vapor streams, wherein - the first source of process vapor stream providing a first process vapor stream is a distillation unit in the first plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material, and
- the second source of process vapor stream providing a second process vapor stream is a purification unit in the first plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material, and
- the third source of process vapor stream providing a third process vapor stream is a transesterification unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO, and
- the fourth source of process vapor stream providing a fourth process vapor stream is a methanol removal unit in the second plant sector of the plant arrangement for the production of poly-THF from THF and AczO.
Within said more preferred plant arrangement according to the present invention, the plant arrangement comprises four evaporators, wherein each of the four evaporators is designed to be fed by feed water at the inlet of the heat output side of the evaporator and to eject a water steam stream at the outlet of the heat output side of the evaporator, and wherein
- the first evaporator is designed to be fed by the first process vapor stream at the inlet of the heat input side, and
- the second evaporator is designed to be fed by the second process vapor stream at the inlet of the heat input side, and
- the third evaporator is designed to be fed by the third process vapor stream at the inlet of the heat input side, and
- the fourth evaporator is designed to be fed by the fourth process vapor stream at the inlet of the heat input side.
It is also preferred that the plant arrangement according to the present invention additionally comprises one, two or more or all of the following plant components (units) - a recirculation conduit designed to recirculate the liquid water phase from the water evaporation unit as feed water to the inlets of the heat output sides of the at least two evaporators,
- one, two or more preheaters for preheating the feed water before it is fed to the inlet of the heat output side of the at least two evaporators, wherein the preheaters are designed to utilize the at least two process vapor streams exiting the at least two evaporators as heating medium,
- valves positioned in front of the inlets of each of the heat output side of the at least two evaporators,
- individual process vapor stream bypass conduits with a control valve positioned in front of the inlets of the heat input side of the evaporators.
The present invention further relates to a target product that can be obtained or achieved by a method according to the present invention.
The publication Prior Art Disclosure; Issue 684; paragraphs [1000] to [8005]; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety. Preferably, the target product is a product as described in Reference RF1 ; paragraphs [1000] to [8005].
Preferably, the process described herein is further a process for the production of a product, preferably a target product. The converting step to obtain the target product preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and/or steam cracking; and/or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and/or subjecting to ion exchanger; and/or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and/or compounding; and/or forming, preferably foaming, extruding and/or molding; and/or finishing, preferably coating and/or smoothing. In addition, the one or more step(s) are described in detail in Reference RF1 ; paragraphs [1000] to [8005]. The term “building block”, as used herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and/or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.
The term “monomer”, as used herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Meth)acrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms.
The terms (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid. The building block can further be an intermediate compound.
The term “intermediate compound”, as used herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and/or diphenylmethane diisocyanate (MDI). The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs [1000] to [1012] of Reference RF1 .
The term “polymer A”, as used herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs [2001 ] to [2007] of Reference RF1 . The term “polymer composition A”, as used herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and/or flame retardant, and is defined in more detail in paragraph [2008] of Reference RF1 .
The term “polymer product A”, as used herein, comprises any product comprising the polymer A and/or polymer composition A as described above and is defined in more detail in paragraphs [2009] and [2010] of Reference RF1 . The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is/are described in more detail in paragraph [201 1 ] of Reference RF1 .
The term “industrial use polymer”, as used herein, comprises rheology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs [3035] to [3044] of Reference RF1 .
The term “industrial use surfactant”, as used herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs [3008] to [3034] of Reference RF1 .
The term “industrial use descaling compound”, as used herein, comprises nonphosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs [3001 ] to [3005] of Reference RF1 .
The term “industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs [3006] to [3007] of Reference RF1 .
The term “industrial use solvent”, as used herein, comprises alkyl amides, alkyllactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs [3045] to [3055] of Reference RF1 .
The term “industrial use dispersant”, as used herein, comprises anionic and nonionic industrial use dispersants defined in more detail in paragraphs [3056] to [3058] of Reference RF1 . The term “composition and/or formulation thereof” with reference to the industrial use polymers, industrial use surfactants, descaling compounds and/or industrial use biocides refers to industrial use compositions and/or institutional use products and/or fabric and home care products and/or personal care products defined in more detail in paragraph [3059] of Reference RF1 . The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3060] of Reference RF1 . The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and/or industrial use biocide are defined in more detail in paragraph [3061 ] of Reference RF1 .
The term “agrochemical composition”, as used herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1 , paragraph [4001 ]. The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mol- let and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer” and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof” may be performed as described in these sections as well as the respective paragraphs in Reference RF1 .
The term active pharmaceutical ingredients and/or intermediates thereof, as used herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient.
The term pharmaceutical excipients, as used herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph [5001 ] of Reference RF1 . The converting step(s) to obtain the active pharmaceutical ingredients and/or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
The terms animal feed additives, human food additives, dietary supplements, as used herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2-propandiol and beverage stabilizers, such as polyvinylpyrroli- done-polymer or polyvinylimidazole/polyvinylpyrrolidone-copolymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph [5002] of Reference RF1 . The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
The terms aroma chemical and aroma composition as used herein, comprise a volatile organic substance with a molecular weight between 70-250 g/mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more detail in paragraph [5003] of Reference RF1 . The converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.
The term “aqueous polymer dispersion”, as used herein, comprises aqueous compositions) comprising dispersed polymer(s) and is defined in more detail in the section [6001 ] entitled “aqueous polymer dispersion” of Reference RF1 . The dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s).
The term “emulsion polymer”, as used herein, comprises polymer(s) made by free- radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section [6002] entitled “Polyurethane dispersions” of Reference RF1 . UV-curable polyurethane(s) is/are defined in more detail in the section [6017] of Reference RF1 . Polyurethane - poly(meth)acrylate hybrid polymer(s) is/are defined in more detail in the section [6016] of Reference RF1 .
The term “polymeric dispersant”, as used herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph [6020] entitled “Polymeric dispersant” of Reference RF1 . The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is/are defined in more detail in the section [6003] entitled “Emulsion polymerization” of Reference RF1 . The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is/are defined in more detail in the section [6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section [6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1 . Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section [6004] entitled “Uses of aqueous polymer dispersions”, section [6005] entitled “Binders for architectural and construction coatings” section [6006] entitled “Binders for paper coating” section [6007] entitled “Binders for fiber bonding” section [6008] entitled “Adhesive polymers and adhesive compositions” section [6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions” section [6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions” section [6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them section [6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use” [6019] 100% curable coating compositions UV-crosslinkable poly(meth)acry- late(s) and its/their uses are defined in more detail in section [6009] entitled “UV- crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hotmelt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1 . Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section [6010] entitled “Polyisocyanates” of Reference RF1 . Hyperbranched polyester polyol(s) and its/their uses are defined in more detail in section [601 1 ] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1 . The converting step(s) to obtain the hyperbranched polyester polyols is/are defined in more detail in the section [6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1 . Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section [6013] entitled “Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1 . Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate^) for coating with said coating composition(s) are defined in more detail in section [6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1 . 100% curable coating composition(s) is/are defined in more detail in section [6019] of Reference RF1 . Polymeric dispersants) for inorganic binder compositions is/are defined in more detail in section [6020] of Reference RF1 . The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section [6021 ] of Reference RF1 . The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section [6020] of Reference RF1 .
The term “inorganic binder composition” comprising the polymeric dispersant(s), as used herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section [6021 ] of Reference RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section [6021 ] of Reference RF1 .
The term “cosmetic surfactant”, as used herein, comprises non-ionic, anionic, cationic, and amphoteric surfactants and is defined in more detail in paragraph [7002] of Reference RF1 .
The term “emollient”, as used herein, refers to a chemical compound used for protecting, moisturizing, and/or lubricating the skin and is defined in more detail in paragraph [7003] of Reference RF1 .
The term “wax”, as used herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph [7004] of Reference RF1 .
The term “cosmetic polymer”, as used herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph [7005] of Reference RF1 .
The term “UV filter”, as used herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph [7006] of Reference RF1 .
The term “further cosmetic ingredient”, as used herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients.
The term “composition and/or formulation thereof” with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and/or further cosmetic ingredient refers to personal care and/or cosmetic compositions or formulations defined in more detail in paragraph [7007] of Reference RF1 . The converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is/are defined in more detail in paragraph [7008] of Reference RF1 .
The terms “polymer B”, “polymer composition B”, “coating composition”, “other functional composition”, “foil”, “molded body”, “coating” and “coated substrate” are well known to the person skilled in the art and are defined in more detail from paragraph [8000] to [8005] of Reference RF1 .
In a preferred embodiment, the target product is selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or
Hi) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyper branched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate. In a preferred embodiment, the content of the polytetrahydrofuran in the target product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight- % or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and/or wherein the content of the polytetrahydrofuran in target product is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and/or segregation and/or mass balance and/or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.
In a preferred embodiment, the preferably above-mentioned embodiments of the method, comprises the step of converting the product of the method, namely polytetrahydrofuran, which can be achieved or obtained by one of the above-mentioned embodiments, to obtain the target product.
EXAMPLES
The following examples according to the present invention are meant to further explain and illustrate the present invention without limiting its scope.
Inventive example 1 :
For the first inventive example a typical middle to large sized process for the production of poly-THF (polytetrahydrofuran) via the intermediate product THF and a typical middle to large sized plant arrangement designed for the production of poly-THF via the intermediate product THF respectively have been considered as base for the simulation carried out. The simulation was performed using Aspen software widely known in the state of the art and commonly used in that cases.
The input data for the simulation was the following:
- a first process vapor stream 101 deriving from an azeotropic distillation in the process stage of producing THF (tetrahydrofuran) from 1 ,4-butanediol with
- a thermal energy of 2.5 MW,
- a lowest temperature of heat transfer of 60 °C,
- a pressure of 1 .10 bara,
- a mass flow of 21 t/h,
- a composition of THF, water and additional byproducts:,
- a second process vapor stream 102 deriving from a purification step in the process stage of producing THF from 1 ,4-butanediol with
- a thermal energy of 2.4 MW,
- a lowest temperature of heat transfer of 65 °C,
- a pressure of 1 .05 bara,
- a mass flow of 25 t/h,
- a composition of almost pure THF,
- a third process vapor stream 103 deriving from a transesterification step in the process stage of producing poly-THF from THF and acetic anhydride (AczO) with
- a thermal energy of 1 .04 MW,
- a lowest temperature of heat transfer of 62 °C, - a pressure of 1 .4 bara,
- a mass flow of 20 t/h,
- a composition of MeAc and MeOH,
- a fourth process vapor stream 104 deriving from a methanol removal step in the process stage of producing poly-THF from THF and AczO with
- a thermal energy of 1 .6 MW,
- a lowest temperature of heat transfer of 62 °C,
- a pressure of 1 .10 bara,
- a mass flow of 4.8 t/h, - a composition of almost pure methanol.
Accordingly, the combined thermal energy of all four process vapor streams was 7.6 MW (heat supplied to the system).
The simulation further assumed that each of the above described four process vapor streams was fed to an evaporator, i.e. four evaporators were present in the simula- tion, and that the evaporators were fed with feed water in order to generate four water steam streams.
The results of the simulation are summarized in Table 1 .
Table 1
* COP = coefficient of performance
As can be seen from the results in table 1 the process I plant arrangement according to inventive example 1 results in 15.1 t/h of water steam generated, i.e. the sum of water steam streams generated by the four evaporators. The power demand (work put into the system) for the evaporators was calculated to be 3.6 MW in total which results in a coefficient of performance (COP) of 3.1 .
The COP was calculated according to the following equation:
COP = Q + W / W, wherein: Q = heat (thermal energy) supplied to the system, and
W = work put into the system.
Inventive example 2:
Inventive example 2 has been simulated with the same parameters as in inventive example 1 with the exception that the process vapor stream 101 was not considered, i.e. the system I simulation was operating with the three process vapor streams 102, 103 and 104 and three evaporators accordingly.
Accordingly, the combined thermal energy of all four process vapor streams was 5.1 MW (heat supplied to the system).
The results of the simulation are summarized in Table 2. Table 2
As can be seen from the results in table 2 the process I plant arrangement according to inventive example 2 results in 10.1 t/h of water steam generated, i.e. the sum of water steam streams generated by the three evaporators. The power demand (work put into the system) for the evaporators was calculated to be 2.4 MW in total which results in a coefficient of performance (COP) of 3.1 , wherein the COP has been calculated as stated above.
These and other aspects of the invention will be apparent from and elucidated with reference to the embodiments described hereinafter with reference to the enclosed drawings. The embodiments of the invention are described in the following on the basis of the drawings in comparison with the state of the art, which is also partly illustrated. The latter is not necessarily intended to represent the embodiments to scale. Drawings are, where useful for explanation, shown in schematized and/or slightly distorted form. With regard to additions to the lessons immediately recognizable from the drawings, reference is made to the relevant state of the art. It should be borne in mind that numerous modifications and changes can be made to the form and detail of an embodiment without deviating from the general idea of the invention. The features of the invention disclosed in the description, in the drawings and in the claims may be essential for the further development of the invention, either individually or in any combination. In addition, all combinations of at least two of the features disclosed in the description, drawings and/or claims fall within the scope of the invention. The general idea of the invention is not limited to the exact form or detail of the preferred embodiment shown and described below or to an object which would be limited in comparison to the object claimed in the claims. For specified design ranges, values within the specified limits are also disclosed as limit values and thus arbitrarily applicable and claimable.
BRIEF DESCRIPTION OF THE DRAWINGS
Further advantages, features and details of the invention result from the following description of the preferred embodiments as well as from the drawings. In the following, a summary of the figures is given.
In the following:
Fig. 1 A is a schematic diagram of the chemical reaction to form tetrahydrofuran (THF) from 1 ,4-butanediol, which is reacted under catalytic conditions;
Fig. 1 B is a schematic diagram of the chemical reaction(s) to form poly-THF starting from THF and AczO (acetic anhydride), including a reaction step wherein MeOH (methanol) is used in a transesterification step;
Fig. 2A is a schematic diagram of the process stage to form tetrahydrofuran (THF) from 1 ,4-butanediol, including individual process steps. Fig. 2A also represents a schematic example for a first plant sector for the production of THF from 1 ,4-butanediol as starting material, including individual plant units;
Fig. 2B is a schematic diagram of the process stage to form poly-THF starting from THF and AczO (acetic anhydride), including individual process steps. Fig. 2B also represents a schematic example for a second plant sector for the production of poly- THF from THF and AczO, including individual plant units;
Fig. 3 is a schematic diagram of a process and/or plant arrangement for the production of poly-THF according to the present invention;
Fig. 4 is a schematic representation of an evaporator for main heat recovery, wherein a process vapor stream is used as heat source to generate a water steam stream from feed water;
Fig. 5 is a schematic diagram of an evaporator positioned in a process vapor stream bypass conduit designed for bypassing a main process vapor stream and also pertains to the preferred embodiment of a preheater; Fig. 6 is a schematic diagram of a source of a process vapor stream in the form of a rectification column.
Fig. 7 is a schematic diagram of a compressor arrangement.
DETAILED DESCRIPTION OF THE DRAWINGS
Fig. 1 A shows the reaction pathway to form tetrahydrofuran (THF) from 1 ,4-butane- diol under catalytic conditions. The reaction can be best described as a ring-forming intramolecular condensation and therefore also gives water as side product which needs to be removed, e.g. in distillation steps.
Fig. 1 B shows the two-step reaction pathway to form poly-THF from tetrahydrofuran (THF). The reaction pathway includes a first step wherein THF is polymerized under the presence of acetic anhydride (AczO) to form poly-THF Diacetate. The second step can be best described as a transesterification reaction, wherein methanol (MeOH) is reacted with poly-THF Diacetate to form poly-THF and AcOMe (or MeAc) as side product which needs to be removed.
Fig. 2A shows the process stage to form tetrahydrofuran (THF) from 1 ,4-butanediol, including individual process steps and shows a schematic example for a first plant sector for the production of THF from 1 ,4-butanediol as starting material, including individual plant units. The specific process steps and plant units include:
- a synthesis step/unit,
- an azeotropic distillation step/unit (wherein water is removed),
- a pressure distillation step/unit,
- a purification step/unit to remove further side products and/or residual starting material and to give THF in high purity. As depicted in Fig. 2A, a first preferred process vapor stream 101 according to the invention is provided in the azeotropic distillation step/unit. A second referred process vapor stream 102 according to the invention is provided in the purification step/unit.
Fig. 2B shows the process stage to form poly-THF starting from THF and AczO (acetic anhydride), including individual process steps and shows a schematic example for a second plant sector for the production of poly-THF starting from THF and AczO, including individual plant units. The specific process steps and plant units include:
- a polymerization step/unit,
- a THF removal step/unit,
- a transesterification step/unit,
- a methanol removal step/unit to give poly-THF in high purity.
As depicted in Fig. 2B, a third preferred process vapor stream 103 according to the invention is provided in the transesterification step/unit. A fourth referred process vapor stream 104 according to the invention is provided in the methanol removal step/unit.
Fig. 3 is a schematic diagram of a process and/or plant arrangement for the production of poly-THF according to the present invention and in detail discloses the parallel arrangement of four evaporators, i.e. a first evaporator 201 , a second evaporator 202, a third evaporator 203 and a fourth evaporator 204. Each of said evaporators is (designed to be) fed with a process vapor stream provided downstream of the process at an inlet of the heat input side (not depicted in Fig. 3). Furthermore, each of the four evaporators is either fed with feed water 401 or bypassed by the feed water 401 by opening or closing the valves 421 , 422, 423 and 424 respectively which are positioned in front of the inlets of the heat output side of the evaporators. The process and/or plant arrangement according to Fig. 3 also comprises a recirculation conduit 410 designed to recirculate the liquid water phase 520 from the water evaporation unit 501 as feed water to the inlets of the heat output sides of the evaporators. Feed water 401 , in particular demineralized water, is fed to inlets of the heat output side of the evaporators for the generation of a first water steam stream 301 on an outlet of the heat output side of the first evaporator 201 , a second water steam stream 302 on an outlet of the heat output side of the second evaporator 202, a third water steam stream 303 on an outlet of the heat output side of the third evaporator 203 and a fourth water steam stream 304 on an outlet of the heat output side of the fourth evaporator 204. Said generated water steam streams 301 , 302, 303 and 304 are combined downstream from the heat output sides of the evaporators and fed to the inlet of a water evaporation unit 501 , in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase 520 and a vapor water phase 510. The vapor water phase downstream from the water evaporation unit 501 is compressed in a compressor arrangement 601 into compressed water vapor of a specific pressure and temperature. The compressed water vapor of a specific pressure and temperature is than fed into a vapor grid 602.
Fig. 4 is a schematic representation of one of the at least two, preferably three or four, “heat cycles” according to the invention. Said singe “heat cycle” comprises a first evaporator 201 for main heat recovery which is fed by a first process vapor stream 101 (used as heat source) to generate a first water steam stream 301 from feed water 401 . Said schematic concept mutatis mutandis applies for the other “heat cycles” according to the invention.
Fig. 5 is a schematic diagram of an evaporator 201 which is fed with feed water 401 and produces a water steam stream 301 and which is positioned in a process vapor stream bypass conduit 701 designed for bypassing a main process vapor stream conduit 720. Accordingly, the evaporator 201 is either fed with the process vapor stream 101 or bypassed by the process vapor stream 101 by opening or closing control valves 71 1 and 721 positioned in front of the inlet of the heat input side of the evaporator in the process vapor stream bypass conduit (valve 71 1 ) and in the main process vapor stream conduit (valve 721 ). According to this “vapor stream bypass concept” the evaporator 201 can either be put into operation or can be left out of the system/process. When the evaporator 201 is bypassed the process vapor stream 101 is usually cooled down in an air cooler 901 . Fig. 5 also shows the concept of an optional preheater 801 wherein feed water 401 is preheated before the feed water 401 is fed to the inlet of the heat output side of the evaporator 201 and wherein the preheater utilizes the remaining thermal energy (heat) of the process vapor stream exiting the evaporator 201 as heating medium.
Fig. 6 shows a preferred source 1 1 1 of a process vapor stream 101 according to the invention in the form of a rectification column or fractionating column. The process vapor stream 101 is fed to the heat input side of an evaporator 201 which is fed with feed water 401 and generates a water steam stream 301 . Said source 1 1 1 may be associated with any of the process steps/units according to the present invention. In particular said source 1 1 1 of a process vapor stream 101 in the form of a rectification column or fractionating column is associated with one of the following process steps/units:
- a distillation unit I step in the first process stage I plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material,
- a purification unit I step in the first process stage I plant sector of the plant arrangement for the production of THF from 1 ,4-butanediol as starting material,
- a transesterification unit I step in the second process stage I plant sector of the plant arrangement for the production of poly-THF from THF and AczO,
- a methanol removal unit I step in the second process stage I plant sector of the plant arrangement for the production of poly-THF from THF and AczO.
The source 1 1 1 preferably provides a process vapor stream 101 with the following set of parameters:
- a temperature of at least 50 °C, preferably is at least 55 °C and/or
- a temperature in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C. and/or
- a pressure in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara.
It is particularly preferred that at least two, preferably two, more preferably four of the process vapor streams according to the invention derive from a source in the form of a rectification column or fractionating column.
Fig. 7 is a schematic diagram of a compressor arrangement 601 . Therein compressor stages are arranged in the form of a compressor cascade of a first, a second and a third compressor C1 , C2, C3, namely as part of a first, a second and a third compressor unit 61 1 , 612, 613. Therein a modelling of the compressor arrangement 601 is shown with the water evaporation unit 501 , which generates a vapor water phase to be fed into the compressor arrangement 601 and a vapor grid 602 which is fed by the compressed water vapor of a specific pressure and temperature as provided by the compressor arrangement 601 .
Herein, the compressor arrangement 601 is provided with a first compressor unit 61 1 , a second compressor unit 612 and a third compressor unit 613, i.e. a “compressor cascade”. The individual compressor units 61 1 , 612 and 613 preferably comprise a steam compressor C1 , C2 and C3 each of all in the form of either a screw compressor or alternatively a radial fan or alternatively an axial turbo compressor.
In particular as shown schematically in Fig. 7, it can advantageously be provided that the live steam is sprayed off in at least one compressor stage, in particular by spraying water in each of the compressor units 61 1 , 612 and 613, however in particular in the first compressor unit 61 1 . Thus, in the compressor cascade, each of the compressor units 61 1 , 612 and 613 respectively combines a first, a second and a third spray nozzle S1 , S2 and S3 with the first, the second and the third compressor C1 , C2 and C3 to respectively provide a compressor unit 61 1 , 612 and 613 as mentioned above for spraying off the live steam. Respective feed water is provided by way of a first, a second and a third pump P1 , P2 and P3 to a respective spray nozzle S1 , S2 and S3.
List of reference signs:
101 first process vapor stream
102 second process vapor stream
103 third process vapor stream
104 fourth process vapor stream
11 1 preferred source of a process vapor stream in the form of a rectification column or fractionating column
201 first evaporator
202 second evaporator
203 third evaporator
204 fourth evaporator
301 first water steam stream
302 second water steam stream
303 third water steam stream
304 fourth water steam stream
401 feed water
410 recirculation conduit designed to recirculate the liquid wa ter phase from the water evaporation unit
421 valve positioned in front of the inlet of the heat output side of the first evaporator
422 valve positioned in front of the inlet of the heat output side of the second evaporator
423 valve positioned in front of the inlet of the heat output side of the third evaporator
424 valve positioned in front of the inlet of the heat output side of the fourth evaporator
501 water evaporation unit
510 liquid water phase from the water evaporation unit
520 vapor water phase from the water evaporation unit
601 compressor arrangement -
602 vapor grid
611 , 612, 613 first, second, third compressor unit, each either as a screw compressor or alternatively a radial fan or alterna tively an axial turbo compressorCI , C2, C3 first, second, third compressor
S1 , S2, S3 first, second, third spray nozzle
P1 , P2, P3 first, second, third pump
701 process vapor stream bypass conduit
711 control valve positioned in front of the inlet of the heat in put side of the evaporator in the process vapor stream bypass conduit
720 main process vapor stream conduit
721 control valve positioned in the main process vapor stream conduit
801 preheater
901 air cooler

Claims

1 . Process for the production of polytetrahydrofuran (poly-THF), wherein
- associated with one, two or more process stages of the process of producing polytetrahydrofuran (poly-THF) at least two process vapor streams are provided downstream of the process, and
- a first process vapor stream is fed to an inlet of the heat input side of a first evaporator of at least two evaporators, and
- a second process vapor stream is fed to an inlet of the heat input side of a second evaporator of at least two evaporators, and
- the first process vapor stream and the second process vapor stream are further used or recirculated in the process from outlets of the heat input side of the first evaporator and the second evaporator, and
- feed water, in particular demineralized water, is fed to inlets of the heat output side of the first evaporator and the second evaporator for the generation of a first water steam stream on an outlet of the heat output side of the first evaporator and a second water steam on an outlet of the heat output side of the second evaporator, and
- the generated first water steam stream and the generated second water steam stream downstream from the heat output sides of the first evaporator and the second evaporator are combined and fed to the inlet of a water evaporation unit, in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase, and
- the vapor water phase downstream from the water evaporation unit is compressed in a compressor arrangement into compressed water vapor of a specific pressure and temperature, in particular is compressed by using electrical energy from a renewable energy source, and
- the compressed water vapor of a specific pressure and temperature is fed into a vapor grid, in particular a heating network.
2. Process according to claim 1 , wherein at least three process vapor streams are provided downstream of the process and wherein - a third process vapor stream is fed to an inlet of the heat input side of a third evaporator, and
- the third process vapor stream is further used or recirculated in the process from an outlet of the heat input side of the third evaporator, and
- feed water, in particular demineralized water, is fed to an inlet of the heat output side of the third evaporator for the generation of a third water steam stream on an outlet of the heat output side of the third evaporator, and
- the generated third water steam stream downstream from the heat output side of the third evaporator is combined with the generated first and second water steam stream downstream from the heat output sides of the first and second evaporator and fed to the inlet of the water evaporation unit, in particular flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase.
3. Process according to any of the preceding claims, wherein at least four process vapor streams are provided downstream of the process and wherein
- a fourth process vapor stream is fed to an inlet of the heat input side of a fourth evaporator, and
- the fourth process vapor stream is further used or recirculated in the process from an outlet of the heat input side of the fourth evaporator, and
- feed water, in particular demineralized water, is fed to an inlet of the heat output side of the fourth evaporator for the generation of a fourth water steam stream on an outlet of the heat output side of the fourth evaporator, and
- the generated fourth water steam stream downstream from the heat output side of the fourth evaporator is combined with the generated first, second and third water steam stream downstream from the heat output sides of the first, second and third evaporator and fed to the inlet of the water evaporation unit, in particular a flash drum, wherein the combined water steam stream undergoes flash evaporation and forms a liquid water phase and a vapor water phase.
4. Process according to any of the preceding claims, wherein the liquid water phase from the water evaporation unit is further used or recirculated, preferably the liquid water phase from the water evaporation unit is recirculated as feed water, which is fed to the inlets of the heat output side of the evaporators.
5. Process according to any of the preceding claims, wherein at least one, preferably all, of the two or more, preferably four, process vapor streams provided downstream of the process derive from the following process steps and process stages:
- distillation step, preferably an azeotropic distillation, in the process stage of producing tetrahydrofuran (THF) from 1 ,4-butanediol,
- purification step in the process stage of producing tetrahydrofuran (THF) from 1 ,4- butanediol,
- transesterification step in the process stage of producing polytetrahydrofuran (poly- THF) from tetrahydrofuran (THF) and acetic anhydride (AczO),
- methanol removal step in the process stage of producing polytetrahydrofuran (poly- THF) from tetrahydrofuran (THF) and acetic anhydride (AczO).
6. Process according to any of the preceding claims, wherein four process vapor streams are provided downstream of the process and wherein
- the first process vapor stream of the four process vapor streams derives from a distillation step, preferably an azeotropic distillation, in the process stage of producing tetrahydrofuran (THF) from 1 ,4-butanediol, and
- the second process vapor stream of the four process vapor streams derives from a purification step in the process stage of producing tetrahydrofuran (THF) from 1 ,4- butanediol, and
- the third process vapor stream of the four process vapor streams derives from a transesterification step in the process stage of producing polytetrahydrofuran (poly- THF) from tetrahydrofuran (THF) and acetic anhydride (AczO), and - the fourth process vapor stream of the four process vapor streams derives from a methanol removal step in the process stage of producing polytetrahydrofuran (poly- THF) from tetrahydrofuran (THF) and acetic anhydride (AczO).
7. Process according to any of the preceding claims, wherein
- the temperature of each of the at least two, preferably four, process vapor streams provided downstream of the process is at least 50 °C, preferably is at least 55 °C and/or
- the temperature of each of the at least two, preferably four, process vapor streams provided downstream of the process is in a range of from 50 °C to 75 °C, preferably in a range of from 55 °C to 70 °C. and/or
- the pressure of each of the at least two, preferably four, process vapor streams provided downstream of the process is in a range of from 0.7 to 2.0 bara, preferably in a range of from 0.9 bara to 1 .5 bara.
8. Process according to any of the preceding claims, wherein the total amount of thermal energy
- of process vapor streams deriving from a process step in the process stage of producing tetrahydrofuran (THF) is at least 1.5 MW per production of 1 kg tetrahydrofuran (THF), preferably is at least 2 MW per production of 1 kg tetrahydrofuran (THF), and/or
- of process vapor streams deriving from a process step in the process stage of producing polytetrahydrofuran (poly-THF)is at least 1.5 MW per production of 1 kg polytetrahydrofuran (poly-THF), preferably is at least 2 MW per production of 1 kg polytetrahydrofuran (poly-THF).
9. Process according to any of the preceding claims, wherein at least one, preferably all, of the at least two, preferably four, evaporators are positioned in individual process vapor stream bypass conduits designed for bypassing a main process vapor stream conduit and are either fed with the process vapor stream or are bypassed by the process vapor stream by opening or closing control valves positioned in front of the inlet of the heat input side of the evaporators in the process vapor stream bypass conduits and in the main process vapor stream conduits.
10. Process according to any of the preceding claims, wherein the feed water is preheated in one, two or more preheaters before the feed water is fed to the inlets of the heat output side of one, two or more of the at least two evaporators and wherein the one, two or more preheaters utilize one, two or more of the at least two process vapor streams exiting the at least two evaporators as heating medium.
11 . Plant arrangement designed for the production of polytetrahydrofuran (poly- THF), comprising
- a first plant sector for the production of tetrahydrofuran (THF) from 1 ,4-butanediol as starting material, and
- a second plant sector for the production of polytetrahydrofuran (poly-THF) from tetrahydrofuran (THF) and acetic anhydride (AczO), and
- at least two separate sources of process vapor streams in the first and/or second plant sector, and
- at least two evaporators in the first and/or second plant sector which are designed - to be fed by a process vapor stream from one of at least two separate sources of process vapor streams in the first and/or second plant sector at the inlet of a heat input side, and
- to be fed by feed water at the inlet of a heat output side, and
- to eject a water steam stream at the outlet of the heat output side, and
- a water evaporation unit, in particular a flash drum, downstream from the heat output sides of the at least two evaporators which is designed
- to be fed by the combined water steam streams from the outlets of the at least two evaporators, and
- to form a liquid water phase and a vapor water phase by flash evaporation of the combined water steam streams, and
- to eject the vapor water phase obtained from the flash evaporation, and
- a compressor arrangement downstream from the water evaporation unit designed
- to be fed with the vapor water phase from the water evaporation unit, and
- to compress the vapor water phase to a specific pressure and temperature, and
- to feed the compressed vapor water phase into a vapor grid, in particular a heating network.
12. Plant arrangement according to claim 1 1 , wherein one, two or more, preferably all, of the at least two, preferably four, separate sources of process vapor streams in the first and/or second plant sector are reactors or columns, preferably rectification columns.
13. Plant arrangement according to claim 1 1 or 12, wherein at least one, preferably all, of the at least two, preferably four, separate sources of process vapor streams are selected from the following process stage units
- a distillation unit in the first plant sector of the plant arrangement for the production of tetrahydrofuran (THF) from 1 ,4-butanediol as starting material,
- a purification unit in the first plant sector of the plant arrangement for the production of tetrahydrofuran (THF) from 1 ,4-butanediol as starting material,
- a transesterification unit in the second plant sector of the plant arrangement for the production of polytetrahydrofuran (poly-THF) from tetrahydrofuran (THF) and acetic anhydride (AczO),
- a methanol removal unit in the second plant sector of the plant arrangement for the production of polytetrahydrofuran (poly-THF) from tetrahydrofuran (THF) and acetic anhydride (AczO).
14. Plant arrangement according to any of claims 11 to 13, comprising
- four separate sources of process vapor streams, wherein
- the first source of process vapor stream providing a first process vapor stream is a distillation unit in the first plant sector of the plant arrangement for the production of tetrahydrofuran (THF) from 1 ,4-butanediol as starting material, and
- the second source of process vapor stream providing a second process vapor stream is a purification unit in the first plant sector of the plant arrangement for the production of tetrahydrofuran (THF) from 1 ,4-butanediol as starting material, and - the third source of process vapor stream providing a third process vapor stream is a transesterification unit in the second plant sector of the plant arrangement for the production of polytetrahydrofuran (poly-THF) from tetrahydrofuran (THF) and acetic anhydride (AczO), and
- the fourth source of process vapor stream providing a fourth process vapor stream is a methanol removal unit in the second plant sector of the plant arrangement for the production of polytetrahydrofuran (poly-THF) from tetrahydrofuran (THF) and acetic anhydride (AC2O), and
- four evaporators, wherein each of the four evaporators is designed to be fed by feed water at the inlet of the heat output side of the evaporator and to eject a water steam stream at the outlet of the heat output side of the evaporator, and wherein
- the first evaporator is designed to be fed by the first process vapor stream at the inlet of the heat input side, and
- the second evaporator is designed to be fed by the second process vapor stream at the inlet of the heat input side, and
- the third evaporator is designed to be fed by the third process vapor stream at the inlet of the heat input side, and
- the fourth evaporator is designed to be fed by the fourth process vapor stream at the inlet of the heat input side.
15. A method for producing a target product by converting the polytetrahydrofuran, which can be obtained or has been obtained according to the process of any one of claims 1 to 10 for the production of polytetrahydrofuran (poly-THF).
PCT/EP2025/066698 2024-07-03 2025-06-16 Process and plant arrangement for the production of polytetrahydrofuran (poly-thf) Pending WO2026008293A1 (en)

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