Method of production of ethylene oxide and plant arrangement adapted for the production of ethylene oxide

Abstract

The invention relates to a method of production of ethylene oxide (EO) and a plant arrangement (1000) adapted for the production of ethylene oxide (EO), wherein in a process for producing ethylene oxide (EO) amongst others: - ethylene oxide (EO) is produced by reacting the reactants including ethylene and oxygen in the presence of a catalyst in a process reactor (R1) in a cycle gas stream (CGS) and a cycle gas (CG) of the cycle gas stream (CGS) at least comprises ethylene oxide (EO), - the cycle gas stream (CGS) is provided to a heat exchanger (W3.1), in particular a heat exchanger (W3.1) in form of a cooler, - the heat exchanger (W3.1) is coupled in a water cooling cycle adapted for cooling the cycle gas stream (CGS) by means of coolant water (CW) of the water cooling cycle (WCC), and - the water cooling cycle (WCC) is coupled to a heat pump cycle (HPC) by providing the coolant water (CW) as a heat source to an evaporator (EVA) adapted for a working fluid (WF) in the heat pump cycle (HPC), and - a steam generating arrangement (SGA) is coupled to the heat pump cycle (HPC) by providing supply water (SW) in the steam generating arrangement (SGA), as a heat sink, to a condenser (CON) for the working fluid (WF) in the heat pump cycle (HPC), wherein - the steam generating arrangement (SGA) is adapted for generating steam (LS, US) from the supply water (SW). A further subject-matter according to the invention is the plant arrangement (1000) for the production of ethylene oxide, comprising a cycle gas arrangement (400) with a process reactor (R1) and a water cooling arrangement (300), a heat pump (100) and a steam generator (200).

Description

[0001] BASF SE

[0002] Carl-Bosch-StraBe 38, 67056 Ludwigshafen am Rhein

[0003] Germany

[0004] Method of production of ethylene oxide and plant arrangement adapted for the

[0005] production of ethylene oxide

[0006] FIELD OF THE INVENTION

[0007] The present invention relates to a process and a plant arrangement for the production of ethylene oxide (EO).

[0008] BACKGROUND OF THE INVENTION

[0009] Ethylene oxide (referred to as “EO” for “ethylene oxide” in the following) can be produced on an industrial scale by direct oxidation of ethylene on a catalyst. The catalyst comprises silver on alumina and other dopants at smaller amounts, or may comprise another suitable catalyst material. Direct oxidation of ethylene on a catalyst is processed with molecular oxygen or with air. Such processes are described, for example, in Ullmann's Encyclopedia of Industrial Chemistry, Fifth Edition, Vol. A 10, pages 117ff.

[0010] According to the above-mentioned kind of process ethylene and oxygen are introduced into a cycle gas stream. In addition to the reactants the cycle gas stream can also comprise inert gases and a by-product of ethylene total oxidation, carbon dioxide as well as other by-products, e.g. aldehydes. As outlined in WO 00 / 17180 A1 further in that kind of process, if necessary, a cooled reactor effluent is quenched first with a NaOH solution to remove organic acids. In particular formic acid and| BASF SE

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[0014] acetic acid as well as heavy-boiling secondary components are washed out. These components can be removed from the circulating gas system via a quench bleed.

[0015] In an ethylene oxide absorber, which is operated at approx. 16 bar and 30 to 40°C, the ethylene oxide is washed out with a large flow of wash water. To absorb 1 t of EO from 25 t of cycle gas approx. 35 t of scrubbing water is required. Usually, ethylene oxide is almost completely washed out of the cycle gas. A pressure in the absorber is determined by the pressure in the cycle gas system. Typically, in the cycle gas 5 to 100 ppm ethylene oxide remains.

[0016] Further in this kind of process, after potash scrubbing to remove carbon dioxide, the cycle gas is enriched again with ethylene and oxygen and fed to the EO reactor. The aqueous solution produced in the absorber also contains traces of the other components contained in the cycle gas.

[0017] Usually, the ethylene oxide is then removed in an ethylene oxide desorber (also referred to as “EO stripper”) wherein the loaded wash water is provided to. The resulting stripper vapors contain approx. 45 wt.% water and approx. 65 wt.% ethylene oxide as well as the gases contained in the loaded wash water.

[0018] Depleted wash water is fed back as circulating water to the ethylene oxide absorber. As the ethylene oxide is partially hydrolyzed to glycols in the ethylene oxide desorber, these are discharged from the ethylene oxide desorber via the so-called glycol bleed. The desorber vapors are first condensed. Then dissolved gases are stripped from the condensate in a column. Thus, further in this kind of process dissolved gases are stripped out of the condensate and returned to the circulating gas system. The gas-free, approx. 65% aqueous ethylene oxide solution obtained in this way is partially purified in a distillation column to obtain pure ethylene oxide or, after the addition of water, is distilled in a glycol reactor to form an aqueous glycol solution.

[0019] A significant proportion of global ethylene oxide production is affected with an increasing processing of monoethylene glycol, hereinafter referred to as glycol. For this purpose, a water / EO mixture with a water / EO mass ratio in the range of approx. 5 to 20 is assumed. The high excess of water is necessary in order to minimize the formation of higher glycols (di-, tri-polyethylene glycols) as far as possible, which are reactions during hydrolysis.| BASF SE

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[0023] Further chemical reaction(s) and conditions for the production of ethylene oxide are disclosed in detail as an example in WO 00 / 17180 A1. Therein a method for the continuous production of an aqueous ethylene oxide solution is described by absorbing ethylene oxide from a gaseous mixture containing 1 .5 to 4 mole percent, preferably 2.5 to 3 mole percent of ethylene oxide in the wash water in an absorber. The mixture drawn directly from the absorber has a water / ethylene oxide weight ratio of 5 to 20, preferably of 10 to 15. The absorbed mixture is especially useful for directly feeding it to a secondary reactor for the production of glycol.

[0024] Also generally, environmental aspects of production of ethylene oxide with improved sustainability are for example disclosed in the article of Faria et al. “Novel ethylene oxide production with improved sustainability: Loss prevention via supersonic separator and carbon capture” as publicized in Journal of Environmental Management 269 (2020) 110782 (https: / / doi.Org / 10.1016 / i.ienvman.2020.110782 ). As described therein ethylene oxide (EO) is a versatile intermediary with high reactivity and flammability issues. Glycols, poly (ethylene oxide), glycol-ethers, ethanolamines, and surfactants are manufactured with EO, a worldwide massively produced chemical with 26*106tons in 2018 and expected 36*106tons in 2023. Due to ethylene oxide toxicity / flammability, ethylene oxide processes have inherent health-safety-environment vulnerability, with environmental burdens from harmful releases, energy-intensity and exergy-destruction. EO life-cycle impact assessment (LCIA) reports climate-change, human-health, ecosystems and particulate-formation concerns.

[0025] Recent works investigated alternative ethylene oxide production routes to mitigate its potential Health-Safety-Environment impacts. As also recited therein e.g. a combined pinch and exergy analysis of an ethylene oxide production process to boost energy efficiency toward environmental sustainability has been attempted. Also titano-silicate / H2O2 catalysts for ethylene oxide synthesis have been investigated. A gas-expanded liquid-based process to reduce carbon dioxide emissions has been studied.

[0026] WO 2011 / 144544 A1 discloses a method for removing carbon dioxide (CO2) from a recycle gas system by means of an absorbent, wherein the CO2 is generated as a by-product within a process in which ethylene is oxidized by oxygen (02) to ethylene oxide (EO) in the gas phase in the presence of a catalyst. An aqueous solution of one or more amines is used as absorbent, wherein, forBASF SE

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[0030] further purification of the recycle gas stream obtained after the CO2 absorption step, it is brought into intimate contact with water to which have not been added a mineral acid or higher glycol.

[0031] Up to now existing plants or plant arrangements for the industrial production of ethylene oxide do not sufficiently utilize the process heat. Such process heat can occur in wash streams, coolant streams, or process streams originating from the chemical reaction steps. On the contrary, most of the existing plants operate with air coolers. Accordingly thermal energy (heat) of process coolant streams is lost or even worse additional energy generated with fossil fuels is needed to cool down process coolant streams.

[0032] At the same time chemical production sites usually rely on heating grids with 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.

[0033] Unused thermal energy in the current production processes and plant arrangements for the production of ethylene oxide and the additional demand of fossil fuels, which are needed to cool down process 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.

[0034] Additionally, current processes for the production of ethylene oxide and the respective plant arrangements for the production of ethylene oxide could become unstable due to the usage of air coolers whose operation can get crucial at high ambient temperature. This or other kind of limited cooling capacity is a bottleneck during summertime and often leads to an unwanted shut-down of the production process or plant arrangement or at least to lowering the production capacity.

[0035] Moreover, a technical problem arises since for many of the wash-, coolant- or process-streams generated in the method of production of ethylene oxide recovering their thermal energy does not seem to be energy efficient. When taken alone the single wash-, coolant- or process- streams have i) a relatively low temperature, ii) a relatively low mass flow and iii) a relatively low thermal energy.

[0036] Accordingly, there is a demand in industry for an improved process and plant arrangement for the production of EO, wherein the process for the production of EO is more energy efficient and prefer-BASF SE

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[0040] ably the emission of greenhouse gases is reduced. Furthermore, unwanted shut-downs of the production process or lowering of the production capacity at high ambient temperature, especially during summer time, shall be avoided.

[0041] Further, to improve the CO2 balance, it has been proven to be of increasingly important to generate green steam using waste heat from a chemical production. Even if a wide variety of methods of using waste heat for energy recovery are generally known, these must regularly be questioned in terms of efficiency as well as technical effort and the feasibility itself or a realistic possibility of integration into existing processes and systems, such as the one mentioned at the beginning.

[0042] Generally, it is particularly questionable if a heat transfer medium with a low heat content only appears to be usable for releasing waste heat into the environment.

[0043] As 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 process industry.

[0044] A heat pump uses existing heat at a low temperature level and transfers it to a higher temperature level using electricity. A suitable heat source is therefore the basic requirement for using a heat pump. In principle, different concepts come into consideration for this: There are restrictions for a large-scale chemical process. In principle, (waste) air or (waste) water, the ground and, in this case, waste heat from production processes, refrigeration systems or cooling systems, combined heat and power plants or from compressed air generation can serve as a heat source.

[0045] The objective is to increase the temperature level of a stream via a heat pump in such a way that the heat of the stream can be used again. The efficiency is determined here via the COP - “Coefficient of Performance” as a measure of the efficiency of a heat pump. The higher the COP value, the more efficiently the heat pump works.

[0046] As described in the article “Use of heat pumps in the chemical industry” by Harald Roth (November 8, 2022) in Chemistry & Technology under Energy & UtilitiesBASF SE

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[0050] ( https : / / www.chemietechnik.de / enerqie-utilities / einsatz-von-waermeDumpen-in-der-chemischen-industrie-788.htm l#:~:text=Doch%20auch%20die%20technisch%20ausqereiften,Trock-nunqs%2D%20Destillations%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 reach up to 160 °C.

[0051] However, such concepts can still be improved in particular with regard to implementation aspects.

[0052] Most concepts for generating heating power of a process steam are currently only suitable to provide fresh steam; i.e. fresh steam with basically undefined parameters or at least depending of the chemical process involved. The fresh steam may also have very low pressure levels of up to 2 bar only and thus could be of limited further use.

[0053] A large part of that kind of fresh steam usually is directly reused as process steam in the further production process, for example for drying products, heating reactors or for distillation. If not defined otherwise a process steam is in particular understood to be in the form of a water steam, i.e. the vapor formed when water changes from the liquid phase to the gas phase.

[0054] Green steam can be understood as a non-polluting source of energy based on process steam.

[0055] Preferably heat recovery is achieved by steam generation and preferably involving renewable energy sources for energy input.

[0056] What is desirable is a concept that can be implemented on a large-scale chemical basis for producing at least process steam, which should be able to be produced as a product using waste heat from the chemical production of EO, in particular as green steam.

[0057] Advantageously, however, the process steam that can be generated in the production of ethylene oxide should be able to be generated as use steam. Unlike fresh steam, the term use steam defines a steam at a defined parameter set of preferably pressure and temperature, at least at a defined pressure; this can be a low-pressure stage or can be generated with higher pressure on a medium-pressure stage or a high-pressure stage.| BASF SE

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[0061] SUMMARY OF THE INVENTION

[0062] It is therefore an object of the present invention to provide an improved method to produce ethylene oxide. Preferably the method is improved by being more energy efficient. Accordingly it is therefore an object of the present invention to provide a plant arrangement for the production of ethylene oxide as a product, wherein the plant arrangement is improved by being operated more energy efficient.

[0063] For an energy efficient production of ethylene oxide at least one process vapor and / or one process steam should be generated. If not defined otherwise a process vapor is in particular to be understood to be in the form of steam, i.e. process steam from water.

[0064] In particular it is the object to produce ethylene oxide in an improved manner wherein heat transfer media should be used and the heat content thereof should be used in an improved manner, namely by means of one or more heat pumps. It is also an object to integrate a heat pump suitably into the chemical reaction process.

[0065] It is in particular an object of the present invention to provide for a method and plant arrangement for the production of ethylene oxide as indicated above, wherein the method and plant arrangement are improved by an advantageous implementation of a heat pump. Preferably the heat pump is adapted to provide heat to produce process steam from supply water.

[0066] Furthermore, the improved method and plant arrangement for the production of ethylene oxide should preferably be able to be integrated into an existing process and plant arrangement and should also be economically attractive.

[0067] In particular, it should be advantageous to incorporate a heat transfer medium into the process of the production of ethylene oxide as disclosed in detail in WO 00 / 17180 A1 mentioned in the introduction, the content thereof is incorporated by reference herein.BASF SE

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[0071] The present invention concerns in its categories a method of production of ethylene oxide and a plant arrangement designed for the production of ethylene oxide. 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.

[0072] 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.

[0073] SUPPORT OF MAIN CLAIMS

[0074] The object is achieved with regard to the method with the features of claim 1.

[0075] The object is achieved by a method of production of ethylene oxide, wherein in a process for producing ethylene oxide:

[0076] (i) at least ethylene and oxygen is provided as parts of reactants to a process reactor for producing ethylene oxide,

[0077] (ii) ethylene oxide is produced by reacting the reactants including ethylene and oxygen in the presence of a catalyst in the process reactor in a cycle gas stream and a cycle gas of the cycle gas stream at least comprises ethylene oxide,

[0078] (iii) the cycle gas stream is provided to a heat exchanger, in particular in form of a cooler,

[0079] (iv) ethylene oxide is washed out of the cycle gas by applying the cycle gas stream to an ethylene oxide absorber column,

[0080] (v) carbon dioxide is washed out of the cycle gas by applying the cycle gas stream to a carbon dioxide absorber column.

[0081] According to the invention in the process:

[0082] (vi) the heat exchanger is coupled in a water cooling cycle adapted for cooling the cycle gas stream by means of coolant water of the water cooling cycle, andBASF SE

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[0086] (vii) the water cooling cycle is coupled to a heat pump cycle by providing the coolant water as a heat source to an evaporator adapted for a working fluid in the heat pump cycle, and

[0087] (viii) a steam generating arrangement is coupled to the heat pump cycle by providing supply water in the steam generating arrangement, as a heat sink, to a condenser for the working fluid in the heat pump cycle, wherein

[0088] (ix) the steam generating arrangement (SGA) is adapted for generating steam from the supply water.

[0089] The invention also leads to a plant arrangement of Claim 9.

[0090] The plant arrangement is adapted for the production of ethylene oxide, in particular the plant arrangement is adapted to operate the method of the invention. The plant arrangement comprises a cycle gas arrangement with a process reactor, in particular a cycle gas loop with a process reactor, wherein in the plant arrangement for production of ethylene oxide,

[0091] (i) the process reactor for producing ethylene oxide is adapted to receive at least ethylene and oxygen as parts of reactants,

[0092] (ii) the cycle gas arrangement is adapted to produce ethylene oxide by reacting the reactants including ethylene and oxygen in the presence of a catalyst in the process reactor in a cycle gas stream and a cycle gas of the cycle gas stream at least comprises ethylene oxide,

[0093] (iii) the cycle gas arrangement has at least one heat exchanger, in particular in form of a cooler, wherein the heat exchanger is adapted to receive the cycle gas stream, in particular with a primary side of the cooler,

[0094] (iv) the cycle gas arrangement has an ethylene oxide absorber column, adapted to receive the cycle gas stream and wash out ethylene oxide of the cycle gas applied to the ethylene oxide absorber column with the cycle gas stream,

[0095] (v) the cycle gas arrangement has a carbon dioxide absorber column, adapted to receive the cycle gas stream and wash out carbon dioxide (CO2) of the cycle gas applied to the carbon dioxide absorber column with the cycle gas stream.

[0096] According to the invention in the plant arrangement:

[0097] (vi) the heat exchanger is coupled in a water cooling cycle adapted for cooling the cycle gas stream by means of coolant water in the water cooling cycle, in particular with a secondary side of the cooler, andBASF SE

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[0101] (vii) a water cooling arrangement is provided with the water cooling cycle is coupled to a heat pump cycle by providing the coolant water, as a heat source, to an evaporator for a working fluid in the heat pump cycle, and

[0102] (viii) a steam generator with a steam generating arrangement is coupled to the heat pump cycle by providing supply water in the steam generating arrangement as a heat sink, to a condenser for the working fluid in the heat pump cycle, wherein

[0103] (ix) the steam generating arrangement is adapted for generating steam from the supply water.

[0104] It is to be understood for a cycle gas loop with the process reactor that -as ethylene oxide is produced by reacting ethylene and oxygen in the presence of a catalyst in the process reactor in a cycle gas stream- the cycle gas comprising ethylene oxide is introduced into the cycle gas stream from the process reactor and also further downflow in a cycle gas loop with the process reactor the cycle gas is reintroduced into the process reactor by again feeding the cycle gas stream to the process reactor. Surprisingly, the concept of the invention has found out that the water cooling cycle can be used as a heat source, having a temperature in a “low temperature” - range. Preferably the temperature in a “low temperature” - range is still above ambient temperature of 30°C, in particular above 40° C but well below 100°C (boiling temperature of water), in particular below 90°C or below 70° C. The water cooling cycle is used as a heat source and thus is of advantageous use for a heat pump such that a water steam can be generated efficiently. Under these conditions, the heat pump has preferably a COP in the range from 2.5 to 3.5.

[0105] Further advantageously the water cooling cycle is relaxed by being coupled to the heat pump cycle and further the temperature amplitude of the water cooling cycle is advantageously damped.

[0106] Energy input to the compressors for the heat pump cycle and / or steam generating arrangement can be provided from regenerative energy sources.

[0107] It is possible to extract heat from the coolant water cycle as explained and supply steam to the plant arrangement preferably in a “green fashion”. If not defined otherwise a process steam as derived from the supply water is in particular to be understood to be in the form of a steam, i.e. the vapor formed when water changes from the liquid phase to the gas phase.BASF SE

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[0111] Green steam or steam generated “in a green fashion” thus can be understood as a non-polluting source of energy based on process steam, i.e. heat recovery by using the heat pump coupled to the watercooling arrangement for steam generation and preferably involving renewable energy sources for energy input.

[0112] Green steam can be understood as a non-polluting source of energy based on process steam, i.e. heat recovery by steam generation and preferably involving renewable energy sources for energy input. Energy sources for energy input to drive the steam compressor of the steam generating arrangement in the steam arrangement or the working fluid compressor in the heat pump need to provide a respective electrical power. Said energy sources of renewable energy can be selected from regenerative sources like solar power, wind power, biomass or geothermal power sources or the like CO2-neutral sources. Unlike fossil energy sources the regenerative sources have the potential to provide clean electric energy.

[0113] Thus, the heat pump in this embodiment is specifically provided as a water-to-water and full cycle heat pump, i.e. applying a full Carnot-Process in the heat pump cycle and coupling thereof to the water cooling cycle as a heat source and the steam generating arrangement as a heat sink. The full cycle heat pump can be understood as a water-to water heat pump as the water cooling cycle is coupled to a heat pump cycle by providing the coolant water, as a heat source, to an evaporator for a working fluid in the heat pump cycle, and a steam generating arrangement is coupled to the heat pump cycle by providing supply water in the steam generating arrangement, as a heat sink, to a condenser for the working fluid in the heat pump cycle. Thus, the heat is taken from coolant water and transferred to the supply water for steam generation.

[0114] The application of a water-to-water and full cycle heat pump stabilizes the cooling mechanisms to the cycle gas stream and relaxes the load in a water cooling cycle applied therein. Further the stabilizing effect is held even at varying environment temperatures, be that it may during cold weather conditions in the winter or heat weather conditions in the summer.

[0115] Further the application of a water-to-water and full cycle heat pump provides options to use at least a part of the steam generated therefrom in the process of processing ethylene oxide (EO) and / or to use at least a part of that steam to feed it into a steam grid.BASF SE

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[0119] SUPPORT OF DEPENDENT CLAIMS

[0120] Advantageous embodiments of the invention are hereinafter found and described in accordance with the dependent claims and indicate in detail advantageous options and embodiments, 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 embodiments of the process and plant arrangement will be described.

[0121] In a preferred embodiment, it is particularly advantageous that carbon dioxide is washed out of the cycle gas by applying the cycle gas stream to a carbon dioxide absorber column.

[0122] In a preferred embodiment, it is particularly advantageously that said first heat exchanging section comprises at least said further heat exchanger in form of a steam generator and / or a still further heat exchanger in form of a “gas-to-gas” - recuperator.

[0123] In a preferred embodiment, it is particularly advantageously that the water cooling cycle is operated in a predetermined temperature range, wherein the heat exchanger in form of the cooler is part of the water cooling cycle. Preferably the heat exchanger thereby is formed as a liquid / liquid heat exchanger operated on the cycle gas between a “middle temperature” - range and a “low temperature” - range. An operation temperature range of the heat exchanger thus is still both below the boiling temperature of water and above ambient temperature - advantageously in a range of between 30°C to 90°C, in particular in a range of between 40°C to 80°C on a primary side in the cycle gas.

[0124] Advantageously the heat exchanger in form of the cooler in the water cooling cycle operates in a “low temperature” - range- in each case well below 100°C (boiling temperature of water), in particular in a range of between 40°C to 70°C at a secondary side in the water cooling cycle.

[0125] In a preferred embodiment, it is particularly advantageously that the steam generating arrangement comprises a first steam generating unit, in particular a condenser secondary side of condenser of the heat pump cycle, for generating fresh steam from the supply water, and

[0126] - a second steam generating unit, for compressing the fresh steam to use-steam of a specified pressure and temperature.BASF SE

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[0130] In a preferred embodiment, it is particularly advantageously that the use-steam is adapted to be used as grid-steam, plant / process-steam or turbine steam.

[0131] In a preferred embodiment, it is particularly advantageously that the heat pump working fluid is a refrigerant selected from the group consisting of butane, in particular n-butane or iso-butane, and ammonia.

[0132] In a preferred embodiment, it is particularly advantageously that the heat pump cycle is operated at a COP in the range from 2.5 to3.5.

[0133] In a preferred embodiment, it is particularly advantageously that

[0134] - supply water supplied to the steam generating arrangement is demineralized and / or de-gassed water, and / or

[0135] - the use-steam is adapted to be used as grid-steam, plant / process-steam or turbine steam.

[0136] In a preferred embodiment, it is particularly advantageously that electric power for working fluid compressor and / or steam compressor is generated from a regenerative energy source.

[0137] In a preferred embodiment, it is particularly advantageously that the steam generating arrangement comprises the condenser,

[0138] - said condenser, in particular with a secondary side of condenser, being adapted as a first steam generating unit for generating fresh steam from the supply water, and

[0139] the steam generating arrangement comprises a steam compressor,

[0140] - said steam compressor being adapted for compressing the fresh steam to use-steam of a specific pressure and temperature.

[0141] In a preferred embodiment, it is particularly advantageous that the steam compressor is a multistage steam compressor, wherein

[0142] - at least one of a number of steam compressor stages comprises a screw compressor, and / or - at least one of a number of steam compressor stages comprises a radial fan,

[0143] - at least one of a number of steam compressor stages comprises an axial turbo compressor.BASF SE

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[0147] In particular, it can advantageously be provided that the fresh steam is sprayed off in at least one compressor stage, in particular by spraying water in at least one compressor stage, in particular the first compressor stage.

[0148] In the order of screw compressors, centrifugal fans, axial turbo compressors, the compressor blades become more sensitive to water droplets. The blades / blades of axial turbo compressors “should not see any water droplets”. There are isolated solutions for screw compressors and centrifugal blowers where water is sprayed in for cooling. Water is usually added to “spray off” the steam after the compressor with the longest possible inlet section. Ideally, the water is sprayed to accelerate evaporation and avoid the formation of droplet streaks.

[0149] In a preferred embodiment, it is particularly advantageously that

[0150] - the heat pump cycle has a working fluid compressor formed as a turbo compressor, in particular in form of a hermetic and / or single shaft turbo compressor, in particular wherein the working fluid in the heat pump cycle is a refrigerant based on butane or comprising butane as a major ingredient, and / or

[0151] - the heat pump cycle has a working fluid compressor formed as a piston compressor, in particular in form of a hermetic piston compressor, in particular wherein the working fluid in the heat pump cycle is a refrigerant based on ammonia or comprising ammonia as a major ingredient.

[0152] In the case the working fluid is a refrigerant based on butane a hermetically sealed compressor is available and thus butane is safely circulated in the heat pump cycle. This advantage prevails even though a refrigerant based on butane may be around 10 % less efficient as compared to a refrigerant based on ammonia. A hermetically sealed turbo compressor advantageously provides for a zero leakage; a loss of refrigerant is avoided. Generally, a variable speed drive control can be provided with the hermetically sealed turbo compressor, which also allows for a quick start-up and shut-down phase. Magnetic bearings avoid a need for lubrication.

[0153] In alternative preferably a single shaft turbo compressor can be provided. This allows at least for a separation unit for oil and refrigerant. Still further preferably this allows for a speed increasing gear box. Also here, the hermetically sealed turbo compressor advantageously provides for a zero leakage; loss of refrigerant is avoided.BASF SE

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[0157] Still there it is preferred to provide safety measures on order to address the rather high flammability of butane.

[0158] As to when working fluid is a refrigerant in form of Ammonia a higher efficiency than butane is achievable in the heat pump cycle and further Ammonia is safely circulated in the heat pump cycle due to its lower flammability. Still, it needs to be addressed toxic aspects of Ammonia and that -as rather turbo compressors are not available with the needed volume flow- smaller machines with piston compressors are available. However, a slight larger machine and additional measures in the cooling and heat pump second cycle are acceptable.

[0159] In a preferred embodiment, it is particularly advantageously that the water cooling cycle comprises a heat exchanger in form of a cooler, in particular with the secondary side of cooler, an air radiator, a pump and an evaporator of the heat pump cycle, in particular with a primary side of evaporator.

[0160] In a preferred embodiment, it is particularly advantageously that the heat pump cycle has the evaporator, in particular with the secondary side of evaporator, a working fluid compressor, the condenser, in particular with the primary side of condenser, and a throttle vent.

[0161] In a preferred embodiment, it is particularly advantageously that a secondary side of evaporator, namely a heat source side of the evaporator, is formed as a flash evaporator wherein the refrigerant is evaporated by means of a forced-circulation flash evaporation or a falling film evaporator wherein the refrigerant is evaporated by means of a falling-film evaporation.

[0162] A forced-circulation flash evaporation is advantageously realized via a flash tank or more advantageously via a heat exchanger. Preferably, a falling film evaporator in form of a “shell and plate” -heat exchanger is used. The falling-film evaporator in an operation mode has a low temperature difference between a temperature of the fluid within its primary side and a temperature of the fluid within its secondary side. Typically, that temperature difference is in the range from 1 °C to 2 °C. The falling film evaporator can also be formed as a “shell and tube”-apparatus.BASF SE

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[0166] Generally, in any of the arrangement, in particular in the steam generating arrangement, a phase separator and a pump is preferably provided. The provision of a phase separator and a pump is advantageous in particular at high mass or water throughputs of several tons per hour.

[0167] EXAMPLES

[0168] The following two examples according to the present invention are meant to further explain and illustrate the present invention without limiting its scope. Both examples assume a heat source in terms of the water cooling cycle at a low temperature range, still above ambient temperature of 30°C but well below a temperature of 100°C (boiling temperature of water), in particular below a temperature of 90°C or below a temperature of 70°C.

[0169] Specifically both examples assume a heat source in terms of the water cooling cycle at a temperature in a low temperature range, in particular of between 45°C and 60°C. Preferably the water cooling cycle operates at a charging flow temperature of 50°C for the cooling water and at a return flow temperature of 57°C for the cooling water; thus with a temperature difference of 7°C. The water cooling cycle provides for a considerable amount of heat of several MW at high mass flow rate of several 10Ot / h.

[0170] Example 1

[0171] Using butane as refrigerant in the heat-pump cycle is capable to operate the heat pump with a COP of around 2.9 to 3.1.

[0172] Fresh steam can be generated at a pressure of around 1.1 bar (here and hereafter barg - bargauge; i.e. gauge pressure values, which are indicated relative to atmospheric pressure) and a temperature of around 110°C thereby; use steam can be generated from the fresh steam in a steam generating arrangement at 2 bar and in the “high temperature” - range at a temperature of above 130°C, preferably around 140°C, at an overall COP of 2.7.

[0173] Example 2

[0174] Using Ammonia as refrigerant in the heat-pump cycle is capable to operate the heat pump with a COP of around 3.2 to 3.3.BASF SE

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[0178] Fresh steam can be generated at a pressure of 1.1 bar and at a temperature of 110°C thereby; use steam can be generated from the fresh steam in a steam generating arrangement at a pressure of 2 bar and in the “high temperature” - range at a temperature of above 130°C, preferably around 140°C, at an overall COP of 2.9.

[0179] 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 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.

[0180] BRIEF DESCRIPTION OF THE DRAWINGS

[0181] 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, wherein it is shown in

[0182] FIG. 1 in view (A) a scheme of the basic method of production and plant arrangement for processing ethylene oxide in cycle gas stream, wherein a heat pump arrangement is coupled with its heat pump cycle to a water cooling cycle related with the cycle gas stream, wherein a water-to-water heat pump type is provided;

[0183] FIG. 1 in view (B) a scheme of the basic concept of the water-to-water heat pump type with a steam compressor as parts of a steam generating arrangement for producing live-steam and use-steam;BASF SE

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[0187] FIG. 2 a scheme of the details of the water-to-water heat pump as shown in the embodiment of FIG. 1 view (A);

[0188] FIG. 3 a detailed overall scheme of the water-to-water heat pump type coupled with its heat pump cycle to a water cooling cycle related with the cycle gas stream in a method of production and plant arrangement for processing ethylene oxide;

[0189] FIG. 4 a scheme of an elaborated method of production and plant arrangement for processing ethylene oxide in cycle gas stream wherein energy from the steam generated in the heat pump and steam generating arrangement is used for heating a column sump;

[0190] FIG. 5 a scheme of the steam compressor in the form of a multi-stage compressor with three stages.

[0191] DETAILED DESCRIPTION OF THE DRAWINGS FIG. 1 view (A) shows a scheme of a preferred embodiment of the method of production of ethylene oxide (referred to as EO in the following) in principle; i.e. in its essential items. Schematically the processing of ethylene oxide (EO) can understood as described in general in Ullmanns’ Encyclopedia. — A more specific method is described in WO 00 / 17180 A1 as is mentioned in the introduction and which is incorporated by reference herein.

[0192] For the production of ethylene oxide (referred to as EO in the following) in a preferred embodiment ethylene and molecular oxygen or air are provided for direct oxidation of the ethylene in a reactor R1. Therein ethylene and the molecular oxygen or air can be provided. Advantageously ethylene and the molecular oxygen or air can be provided therein on a suitable catalyst, preferably a catalyst comprising a silver or silver based catalyst material. In particular ethylene and the molecular oxygen or air can be provided on a silver catalyst, to process ethylene oxide EO by preferably partial oxidation. The reactor R1 itself can be provided as a tube bundle reactor loaded with a silver catalyst material for advantageously partial oxidation of ethylene and oxygen to ethylene oxide EO.

[0193] It is to be understood for a cycle gas loop with the process reactor R1 that -as ethylene oxide EO is produced by reacting ethylene and oxygen in the presence of a catalyst in the process reactor R1BASF SE

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[0197] in a cycle gas stream CGS- the cycle gas CG comprising ethylene oxide is introduced into the cycle gas stream CGS from the process reactor R1 and also further downflow in a cycle gas loop with the process reactor R1 the cycle gas CG is reintroduced into the process reactor R1 by again feeding the cycle gas stream CGS to the process reactor R1.

[0198] This being understood, ethylene oxide EO is introduced into a cycle gas stream CGS in a cycle gas arrangement 400 of a cycle gas loop with the process reactor R1. The cycle gas CG comprising ethylene oxide EO is introduced into the cycle gas stream CGS with a certain specified pressure and temperature at a throughput of demand. The cycle gas stream CGS comprises the reactants ethylene and molecular oxygen or air. The cycle gas stream CGS may contain in addition to the reactants, inert gases and the byproduct of ethylene partial or total oxidation. The main byproduct is carbon dioxide. Consequently the cycle gas stream CGS is also referred to as a loaded cycle gas stream CGS.

[0199] At a reactor outlet the circulation of the cycle gas CG in the cycle gas stream CGS is provided at an exaggerated temperature of well above the boiling temperature of water, in particular the temperature amounts to several 100°C. It can be understood that the gaseous mixture provides for predominantly ethylene and methane and in minor parts ethyl chloride and oxygen and ethylene oxide and further inert gases.

[0200] The cycle gas stream CGS is provided to a heat exchanger W3.1 , in particular a heat exchanger W3.1 in form of a cooler. More specifically the cycle gas stream CGS is provided to an upstream heat exchanging section, which in this embodiment is a first one of two heat exchanging sections W1 , W2.

[0201] The first and / or second heat exchanging sections W1 , W2 each alone or in combination can be provided in various forms. The first and / or second heat exchanging section W1, W2 each alone or in combination generally can be considered to provide a cooling to the cycle gas CG.

[0202] In the preferred embodiment the first heat exchanging section W1 comprises a first heat exchanger W1.1 in the form of a steam generator. Further, in the instant embodiment the second heat exchanging section W2 comprises a second heat exchanger W2.1 in the form of a “gas-to-gas” - recuperator.BASF SE

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[0206] Thereafter, in a sequence, the cycle gas stream CGS is provided for aftercooling to a heat third heat exchanging section W3.

[0207] The third heat exchanging section W3 generally can be considered to provide an aftercooling section; in other embodiments it can be formed in various ways without departing from the spirit of the instant invention. In the instant embodiment the third heat exchanging section W3 comprises a third heat exchanger W3.1 in the form of a cooler.

[0208] Whereas the cycle gas stream CGS in principle has said exaggerated temperature when leaving the reactor R1 , the cycle gas stream is cooled down to a “middle temperature” - range. A temperature of the cycle gas stream in the middle temperature” - range is still well below 100°C (boiling temperature of water), in particular below 90°C or below 80°C when the cycle gas stream is introduced into the heat exchanging section W3 for aftercooling. The heat exchanging section W3 provides for further aftercooling of the cycle gas stream CGS from said “middle temperature” - range to a temperature in a “low temperature” - range. A temperature of the cycle gas stream in the “low temperature” - range is still above ambient temperature of 30°C and preferably below 80°C.

[0209] These values of temperatures T and respective pressures p for the cycle gas stream CGS at the upstream heat exchanging section W1 , W2 and the third downstream heat exchanging section W3 may vary depending on the specific process applied and peripheral circumstances. Various other embodiments may be specified without departing from the spirit of the invention.

[0210] According to the invention three temperature ranges can be defined. A first temperature range of said temperature ranges can be defined in terms of an exaggerated temperature well above a boiling temperature of water which applies to the cycle gas stream CGS at the exit of the reactor. A second temperature range of said temperature ranges can be defined in terms of a “middle temperature” - range below the boiling temperature of water which applies to the cycle gas stream CGS at the after-cooler. A third temperature range of said temperature ranges can be defined in terms of a “low temperature” - range below the boiling temperature of water which applies to the water cooling cycle WCC.

[0211] According to the invention the heat pump cycle works at a working temperature in a “high temperature” - range between a lower temperature well below the boiling temperature of water and an up-BASF SE

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[0215] per temperature well above the boiling temperature of water. Thus basically said working temperature is between the low temperature below the boiling temperature of water of the coolant water CW in the water cooling cycle WCC and the high temperature above the boiling temperature of water of the fresh steam FS generated in the steam generating arrangement SGA.

[0216] According to the concept of the invention, in the method of production of ethylene oxide EO at least ethylene E and oxygen O is provided to the process reactor R1 for producing EO and ethylene oxide EO is produced by reacting the reactants including ethylene and oxygen in the presence of a catalyst in the process reactor R1 in the cycle gas stream CGS and a cycle gas CG of the cycle gas stream CGS at least comprises ethylene oxide EO. Then the cycle gas stream CGS is provided to a heat exchanger W3.1 , in particular a heat exchanger (W3.1) in form of a cooler.

[0217] Upstream the cycle gas stream CGS is provided to one or more upstream heat exchanging sections W1 , W2 and downstream the cycle gas stream CGS is provided to the further (in this embodiment third) heat exchanging section W3. Said third heat exchanging section W3 comprises said heat exchanger W3.1 in form of said cooler, which in this embodiment is adapted to provide an aftercooling to the cycle gas stream CGS.

[0218] The heat exchanger W3.1 in form of said cooler in the specific embodiment shown in FIG. 1 view (A) is an aftercooler as a part of the heat exchanger section W3 as described above.

[0219] The cooler as a part of the heat exchanging section W3 provides heat-coupling to a water cooling cycle WCC with coolant water as shown in principle in FIG. 1 view (A).

[0220] FIG. 1 view (B) depicts in principle a full cycle heat pump 100 coupled to the cycle gas stream CGS in the cycle gas arrangement 400 by means of the coolant water CW in the water cooling cycle WCC.

[0221] According to the concept of the invention the heat exchanger W3.1 is coupled in a water cooling cycle adapted for cooling the cycle gas stream CGS by means of coolant water CW of the water cooling cycle WCC. The water cooling cycle WCC will be described further down in detail with reference to FIG. 3. The cycle gas stream CGS with the cycle gas CG is provided to a primary side 410 of the heat exchanger W3.1. The heat exchanger W3.1 is in form of the cooler as shown inBASF SE

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[0225] FIG. 3, wherein the cooler is explained to be part of the water cooling cycle WCC. The water cooling cycle WCC is adapted for cooling the cycle gas CG of the cycle gas stream CGS by means of coolant water CW of the water cooling cycle WCC.

[0226] In this particular embodiment, as shown in FIG. 1 view (A) and FIG. 1 view (B), the coolant water CW is indicated by the symbol H2O. Thus, as described above and shown in detail in FIG. 1 view (A), the cycle gas stream CGS is provided to a cooler of the water cooling cycle WCC for cooling the cycle gas CG by means of coolant water of the water cooling cycle WCC.

[0227] Once the third heat exchanging section W3 efficiently cools down the cycle gas CG of the cycle gas stream CGS to a preferred temperature T. Therein the preferred temperature T is around 40 °C or below thereof.

[0228] Ethylene oxide EO is washed out of the cycle gas CG by applying the cycle gas stream CGS to an ethylene oxide absorber column K1. The loaded cycle gas stream CGS comprising ethylene oxide EO is provided to a first absorption unit K1. In this embodiment the first absorption unit K1 is formed as an absorption column as an ethylene oxide absorber column. The first absorption unit K1 is adapted to absorb ethylene oxide EO from the cycle gas CG. Thereby loaded cycle water (H2O) is provided as a product stream comprising or being enriched with ethylene oxide EO - the ethylene oxide EO is provided as a product from the loaded cycle water (H2O) as a product stream.

[0229] Carbon dioxide (CO2) is washed out of the cycle gas CG by applying the cycle gas stream CGS to a carbon dioxide absorber column K2. Thus further, the cycle gas CG of the cycle gas stream CGS, is provided to a second absorption unit K2. Therein the second absorption unit K2 is formed as an absorption column as a carbon dioxide absorber column. Thus the second absorption unit K2 is adapted to wash out carbon dioxide CO2 from the cycle gas CG by applying the cycle gas stream CGS to a carbon dioxide absorber of the second absorption unit K2. From the second absorption unit K2, a carbon dioxide loaded scrubbing solution is branched off for further processing as will be apparent from FIG. 4 explained further below.

[0230] Thereafter, the remaining cycle gas CG of the cycle gas stream CGS is further introduced into the reactor R1. The reactor R1 thus is loaded with cycle gas CG of the cycle gas stream CGS and further with ethylene and oxygen as described above.BASF SE

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[0234] Thus, at least from the ethylene oxide EO produced, ethylene oxide EO is washed out of the cycle gas CG by applying the cycle gas stream CGS to the first absorption unit K1 as an ethylene oxide absorber. Further the cycle gas CG is reintroduced into the process reactor R1 by applying in a cycle the cycle gas stream CGS to the process reactor R1.

[0235] As is indicated in FIG. 1 view (B) the water cooling cycle WCC in this embodiment is coupled to the third heat exchanger section W3 or as a part thereof and is further coupled to a heat pump cycle HPC; namely to constitute a heat pump 100.

[0236] As will be explained with reference to the further figures the water cooling cycle WCC is coupled to a heat pump cycle HPC by providing the coolant water CW as a heat source to an evaporator EVA adapted for a working fluid WF in the heat pump cycle HPC. In the water cooling cycle WCC the coolant water CW is provided to an evaporator EVA for a working fluid WF of the heat pump cycle HPC. The heat pump cycle HPC as such is further shown in detail in FIG. 1 view (B).

[0237] Thus, the working fluid WF of the heat pump cycle HPC, is circulating in the heat pump cycle HPC to extract heat from the coolant water CW of the water cooling cycle WCC by means of the evaporator EVA. Consequently, the coolant water CW provides a heat source to the working fluid WF in the heat pump cycle HPC.

[0238] Further, the heat pump cycle HPC provides for a condenser CON also shown schematically in FIG.

[0239] 1 view (B) to constitute the heat pump 100. The working fluid WF is cooled down in the condenser CON of the heat pump cycle. In particular the working fluid WF is cooled on a primary side 130 of the condenser CON and further delivers heat to a steam generating arrangement SGA. The condenser CON is shown schematically in FIG. 1 view (B) being part of the steam arrangement 200 as further shown in FIG. 2.

[0240] To be more specific, the condenser CON, in particular a secondary side 210 of the condenser CON, and a compressor arrangement COM are both part of the steam generating arrangement SGA. In other words, essentially according to the concept of the invention, the steam generating arrangement SGA is coupled to the heat pump cycle HPC by providing supply water SW to the condenser CON. This arrangement is adapted to generate steam from supply water SW by extracting heat from the working fluid WF of the heat pump cycle HPC in the primary side 130 of the condenser CON and thereby condensing the working fluid WF in the heat pump cycle HPC, whilstBASF SE

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[0244] transporting the heat extracted from the working fluid WF to the secondary side 210 of the condenser CON.

[0245] The supply water SW in the steam generating arrangement SGA herein is depicted as H2O and is provided as demineralized and / or degassed water (also referred to as VE-water) to the condenser CON, namely to the secondary side 210 of the condenser CON. Thus, according to the concept of the invention, the supply water SW serves to generate steam in the condenser CON and serves as a heat sink to the heat pump cycle HPC by absorbing the heat extracted from the working fluid WF.

[0246] Even more specifically, in the heat pump cycle HPC, the working fluid WF receives heat from the coolant water CW of the coolant water cycle SCC as a heat source. I In turn the supply water SW of the steam generating arrangement SGA receives heat from the working fluid WF and thus serves as the heat sink. Consequently, the full cycle heat pump 100 can be considered as a “water-to-water”-heat pump 100.

[0247] A steam generating arrangement SGA is coupled to the heat pump cycle HPC by providing supply water SW in the steam generating arrangement SGA, as a heat sink, to a condenser CON for the working fluid WF in the heat pump cycle HPC, wherein the steam generating arrangement SGA is adapted for generating steam LS, US from the supply water SW. The heat received by the supply water SW in the steam arrangement 200 is sufficiently large to generate steam from the supply water SW in the steam generating arrangement SGA.

[0248] More specifically as further shown in FIG. 1 view (B) and FIG. 2, the supply water SW is provided to the condenser CON to generate fresh steam FS in the condenser CON. Therein the fresh steam FS further is provided to the compressor COM to compress the fresh steam FS to a specified pressure and temperature. In other words, the steam generating arrangement SGA comprises the condenser CON which is adapted as a first steam generating unit for generating fresh steam FS from the supply water SW. As being further indicated in FIG. 1 view (B) the steam compressor COM is adapted for compressing the fresh steam FS to use steam US of a specified pressure and temperature T.

[0249] Turning to FIG. 2, the heat pump cycle HPC is shown in more detail. The heat pump cycle HPC with the evaporator EVA and the condenser CON also can be considered as a full cycle heat pumpBASF SE

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[0253] 100. The heat pump 100 in the heat pump cycle thus comprises a secondary side 110 of the evaporator EVA, for evaporation of the working fluid WF.

[0254] Consequently the working fluid WF in the heat pump cycle HPC undergoes a full cycle of transformation, which can -at least theoretically- be considered as a full cycle of a Carnot-Process starting from a liquid phase of the working fluid WF.

[0255] I.e. at first the evaporation of the working fluid WF in the evaporator EVA along with an (basically adiabatic) expansion of the working fluid WF.

[0256] At second this is followed by a (basically isothermal) compression of the working fluid WF in the fluid compressor 120 in the heat pump cycle HP.

[0257] Then, as explained above at third, this is followed by a (basically adiabatic) compression of the working fluid WF due to condensation of the working fluid WF as the working fluid WF is cooled down in the condenser CON of the heat pump cycle HPC.

[0258] Finally, at fourth, a full transforming of the working fluid WF to its starting condition is achieved in a (basically isothermal) expansion in a throttling valve 140 in the heat pump cycle HPC for expanding the working fluid WF. Therefore the working fluid WF is cooled down again to its original temperature.

[0259] The heat source side, i.e. the primary side 320 of the evaporator EVA in the cooling cycle WCC couples to the heat pump cycle HPC. The cooling cycle WCC constitutes a heat source to the heat pump cycle HPC, i.e. as explained above, by exchanging heat of the coolant water CW and providing the heat of the coolant water CW to the working fluid WF in the secondary side 110 of the evaporator EVA in the heat pump cycle HPC. Further the steam generating arrangement SGA constitutes a heat sink coupled to the heat pump cycle HPC by the condenser CON, as explained above, by exchanging heat of the working fluid WF and providing the heat of the working fluid WF to the supply water SW in the condenser CON. -As explained above the condenser CON is a part of the steam generating arrangement SGA. Given the above operation of the heat pump cycle HPC it is coupled to the cooling cycle WCC and the steam generating arrangement SGA, Consequently, the heat pump cycle HPC can be considered as full cycle heat pump 100 with heat pump cycle HPC, cooling cycle WCC and steam generating arrangement SGA.BASF SE

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[0263] The evaporator EVA, namely a secondary side 110 of the evaporator EVA, is in this embodiment a flash-tank. However, also a falling film evaporator can be provided therein as suitable for evaporation of the working fluid WF by means of said forced-circulation flash evaporation or falling film evaporation. Thus, the heat source side of said evaporator EVA can be found as a flash or falling film evaporator. Therein the refrigerant is evaporated by means of a forced -circulation flash evaporation or falling film evaporation. Supplemented to above-mentioned FIG. 2, the heat sink side condenser CON is preferably formed as a falling film evaporator, wherein the supply water SW is gasified to provide fresh steam in a falling film evaporation.

[0264] In a preferred embodiment, the refrigerant is butane, wherein the heat pump cycle has a working fluid compressor 120 of the heat pump cycle HPC which is formed as a turbo compressor. A turbo compressor is in particular advantageously formed as a hermetic compressor. Such hermetic compressor can preferably be formed as a single-shaft turbo compressor.

[0265] In an alternative, in particular when the refrigerant is ammonia, the heat pump cycle has a working fluid compressor 120 formed as a piston compressor. Also said piston compressor can particularly be formed as a hermetic compressor.

[0266] The working fluid WF of this embodiment is a refrigerant in the form of butane in a first variant or ammonia in a second variant. Both, the refrigerant butane or the refrigerant Ammonia, are evaporated in the evaporator EVA from taking the heat of the coolant water CW, thereby cooling down the coolant water from a low in-temperature “in-T” to a low out-temperature “out-T” in the “low temperature” - range.

[0267] The gaseous working fluid WF in the form of gaseous refrigerant then -as mentioned above- is provided to a working fluid compressor 120 in the heat pump cycle HPC of the heat pump 100.

[0268] The working fluid WF compressor 120 is powered by electrical power P_el in this specific embodiment- Thereby the refrigerant of the working fluid is compressed and further heated up into a gaseous form of the refrigerant as the working fluid.

[0269] Further, in the sequence of the pump cycle HPC, the working fluid in the form of refrigerant as mentioned above is condensed in the condenser CON, more specifically on the primary side 130 of the condenser CON. Thereby, the working fluid WF is returned from the gaseous refrigerant phase to aBASF SE

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[0273] liquid refrigerant phase and thus providing heat in the condenser CON to the supply water SW in the steam generating arrangement SGA, more specifically on the secondary side 210 of the condenser CON.

[0274] Finally, in the heat pump cycle HPC of the heat pump 100, the liquefied working fluid WF as a refrigerant from the condenser CON is provided to a throttling valve 140 in the heat pump cycle HPC for expanding the working fluid WF and therefore cooling down the working fluid WF again to its original temperature; thus ready to receive heat from the coolant water CW as described above.

[0275] In turn, the steam generating arrangement SGA hereinafter also is referred to with reference mark 200. The steam generating arrangement SGA comprises the condenser CON, more specifically the secondary side 210 of the condenser CON, and a steam compressor 220. The “supply water and steam” - side of the steam generating arrangement SGA hereinafter is referred to as reference mark 210. The “supply water and steam” - side of the steam generating arrangement SGA forms the secondary side of the condenser CON. The secondary side of the condenser CON is constructed in co-ordination with the primary side 130 of the condenser CON for heat exchange. The primary side 130 and secondary side 210 of the condenser CON are adapted for heat exchange in operation.

[0276] In operation and in order to carry out the heat exchange the primary side 130 of the condenser CON is subjected to a flow of a working fluid WF and the secondary side 210 of the condenser CON is subjected to a flow of a supply water SW. Due to transfer of heat to the secondary side 210, said supply water SW absorbs the heat and evaporates, i.e. said supply water SW undergoes a phase change and is turned to water steam. Thus, the process steam from the supply water SW in this embodiment is to be understood to be in the form of a water steam, i.e. the water steam is constituted by vapor formed when the supply water SW changes from the liquid phase to the gas phase.

[0277] Green steam can be understood as a non-polluting source of energy based on process steam, i.e. heat recovery by using the heat pump 100 coupled to the watercooling arrangement 200 for steam generation and preferably involving renewable energy sources for energy input. Energy sources for energy input to drive the aforementioned steam compressor COM, 220 of the steam generating arrangement SGA in the steam arrangement 200 or the aforementioned working fluid compressor 120 in the heat pump 100 are demanded to provide a respective electrical power P_el. Said EnergyBASF SE

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[0281] sources of renewable energy can be selected from regenerative sources like solar power, wind power, biomass or geothermal power sources or the like CO2-neutral sources. Unlike fossil energy sources the regenerative sources have the potential to provide clean electric energy.

[0282] The heat Q2 extracted from the working fluid as refrigerant on the secondary side 210 of the condenser CON is used to generate fresh steam FS at a pressure of or above 1.1 bar and at a temperature of or above 110 °C in this specific embodiment.

[0283] The fresh steam FS is provided to a steam compressor 220 to produce, in this embodiment in the multi-stage compressor COM, use steam US as indicated in FIG. 2 and as will be further explained with FIG. 5.

[0284] The multi-stage steam compressor COM herein is powered electrically and produces steam of specific pressure and temperature as use steam US, wherein the pressure amounts to basically 2 bar at a temperature in the “high temperature” - range well above the boiling temperature of water - in this example the temperature of the use steam US is at 140 °C.

[0285] A coefficient of performance COP is considered to be a relationship between power (KW) that is drawn out of the heat pump 100 as cooling or heat (output) and the power (KW) that is supplied to the compressor (input). Based thereon, the coefficient of performance COP of the heat pump 100 in this embodiment is calculated to a COP_HP in a range between 2.9 and 3.3 -when taking into account the driving of the multi-stage steam compressor- an in total coefficient of performance COP_total is in the range of between 2.6 and 3.0.

[0286] The instant embodiment of the heat pump 100 advantageously provides that the heat pump cycle HPC is coupled to the water cooling cycle WCC, by means of the coolant water CW transferring heat from the water cooling cycle WCC to the heat pump cycle HPC. Thus, the heat pump cycle HPC is not directly coupled to the the cycle gas stream CGS for heat transfer, but only the water cooling cycle WCC is coupled the cycle gas stream CGS.

[0287] Thus, the heat pump 100 in this embodiment is specifically provided as a water-to-water and full cycle heat pump, i.e. applying a full Carnot-Process in the heat pump cycle HPC and coupling thereof to the water cooling cycle WCC as a heat source and the steam generating arrangement SGA as a heat sink.BASF SE

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[0291] The full cycle heat pump 100 can be understood as a water-to water heat pump as the water cooling cycle WCC is coupled to the heat pump cycle HPC by providing the coolant water CW -as a heat source- to an evaporator EVA for a working fluid WF in the heat pump cycle HPC. Also a steam generating arrangement SGA is coupled to the heat pump cycle HPC by providing supply water SW in the steam generating arrangement SGA -as a heat sink- to a condenser CON for the working fluid in the heat pump cycle HPC. Thus, the heat Q1 as shown in FIG. 3 is taken from coolant water CW and transferred to the supply water SW for steam generation with increased energy content in terms of heat Q2 and heat Q3 respectively as shown in FIG. 3.

[0292] The application of a water-to-water and full cycle heat pump stabilizes the cooling mechanisms to the cycle gas stream CGS and relaxes the load in the water cooling cycle WCS applied therein. Further the stabilizing effect is held even at varying environment temperatures, be that it may during cold weather conditions in the winter or heat weather conditions in the summer.

[0293] FIG. 3 thus shows in detail -as explained with FIG. 1 view (A)- the water cooling cycle WCC as one form or part of the third exchanging section W3; the water cooling cycle WCC herein-after is also referred to with the water cooling arrangement 300. The reference marks as indicated in FIG. 1 and FIG. 2 are also shown in FIG. 3 for the same features and specifically the water cooling cycle WCC is explained in FIG. 3.

[0294] The water cooling cycle WCC, respectively the water cooling arrangement 300, provides for said heat exchanging section W3 with heat exchanger W3.1. The secondary side 310 of the heat exchanger W3.1 for flow of coolant water CW in the heat exchanging section W3 is part of the water cooling cycle WCC. Therein the primary side 410 of the heat exchanger W3.1 in form of the cooler is part of the cycle gas arrangement 400 as shown in FIG. 1 view (A) for flow of cycle gas CG in the cycle gas stream CGS. The cycle gas arrangement 400 will be explained in more detail in FIG. 3 and follow-up FIG. 4.

[0295] Further turning to FIG. 3, the water cooling cycle WCC, respectively the water cooling arrangement 300, also comprises provides for said evaporator EVA whose primary side 320 hereinafter is referred to for through flow of coolant water CW, whereas the secondary side 110 of said evaporator EVA is adapted for through flow of working fluid WF in the heat pump cycle HPC as explained with FIG. 2.BASF SE

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[0299] It should be noted that thereby the coolant water CW in the primary side 320 of the evaporator EVA, is cooled down from a low in -temperature “in-T” to a low out-temperature “out-T” in the “low temperature” - range.

[0300] Further turning to FIG. 3, the coolant water CW in the water cooling cycle WCC of water cooling arrangement 300 is cooled down in a radiator 330, wherein the temperature of the coolant water CW is further lowered well below the low out-temperature “out-T”, preferably to a temperature cooled down at ambient or room temperature at the lower margin of the “low temperature” - range.

[0301] Further, in the water cooling cycle of the water cooling arrangement 300, a pump 340 is provided for supporting circulation of through flow of coolant water CW in the water cooling cycle to the secondary side 310 of the heat exchanger W3.1 in form of a cooler. The heat exchanger W3.1 , namely the cooler, preferably forms a third exchanging section W3 in the cycle gas stream CGS or is part of the third exchanging section W3 in the cycle gas stream CGS. The heat exchanger W3.1 has a primary side 410 in the cycle gas stream CGS, which is subject to a through flow of cycle gas CG.

[0302] As explained with FIG. 1 view (A), at this process step, the cycle gas CG preferably has already lost temperature from an exaggerated temperature to a temperature in the “middle temperature” -range. The cycle gas CG is cooled down in the heat exchanger W3.1 of the heat exchanging section W3 to an even lower temperature, still above ambient temperature, in the cycle gas stream CGS of the cycle gas arrangement 400. The cycle gas CG in a down flow direction from the third heat exchanging section W3 is provided to say absorption unit K1 in the form of an absorption column as an ethylene oxide absorber column. Thus, the primary side 410 of the heat exchanger W3.1 in the form of a cooler of the third exchanging section W3 in this embodiment is part of the cycle gas arrangement 400. The cycle gas arrangement 400 also comprises the first and second absorption unit K1 , K2 and the reactor R1 as explained with FIG. 1 view (A).

[0303] Further referring to FIG. 3, the overall plant arrangement 1000 is shown for the production of ethylene oxide EO with above-mentioned cycle gas arrangement 400 adapted to provide said cycle gas stream CGS of cycle gas CG comprising the ethylene oxide plant product gas stream. For good order, the same reference marks are used for the same or similar features as mentioned above and respective description of said features apply also to FIG. 3.BASF SE

[0304]

[0305] 240181

[0306]

[0307] Further, the plant arrangement 1000 comprises said water cooling cycle WCC in said water cooling arrangement 300.

[0308] The water cooling arrangement 300 is coupled to above-mentioned heat pump 100 by means of the evaporator EVA, wherein the primary side 320 of the evaporator EVA is adapted for a through flow of coolant water CW and the secondary side 110 of the evaporator EVA is adapted for through flow of working fluid WF in the form of a refrigerant like butane or ammonia. The details of the heat pump 100 providing for the heat pump cycle HPC are depicted with FIG. 2 as explained above.

[0309] Thus, the heat pump 100 in this embodiment is specifically provided as a water-to-water and full cycle heat pump 100.

[0310] The heat pump 100 is coupled to the steam generator 200 providing for the steam generating arrangement SGA in the form of the secondary side 210 of the condenser CON in heat exchanging coupling to the primary side 130 of the condenser CON.

[0311] In the secondary side 210 of the condenser CON, supply water SW is gasified to steam in the form of fresh fresh steam fresh steam FS. The fresh steam fresh steam FS is further compressed by a multi-stage steam compressor COM which is also referred to as compressor 220 herein below as part of a steam generating arrangement.

[0312] FIG. 4 shows in more detail the plant arrangement 1000, providing the essential parts of the plant arrangement 1000 as shown with FIG. 1 view (A). It should be noted that the cycle gas steam with the cycle gas CG is basically the same as shown FIG. 1 view (A) except for the fact that the first heat exchanging section W1 is further specified.

[0313] The upstream heat exchanging section comprises a steam generator W1.1 and a “gas-to-gas” - recuperator W2.1 in sections W1 , W2. Further, the same reference marks are used as in view (A) of FIG. 1 and respectively the description thereof also applies here.

[0314] In addition, from the first and second absorption unit K1 , K2, respectively ethylene oxide is derived as product and CO2 as a side product respectively.BASF SE

[0315]

[0316] 240181

[0317]

[0318] Therein stripping of CO2 from the scrubbing solution is provided in a further column K3, the column sump of the stripping column K3 is coupled to a heat exchanging section W4 which preferably is operated in a (p,T)-operation condition at raised pressure and well above the 100°C.

[0319] Thus, the use steam US generated from the heat pump arrangement 100 --comprising the heat pump cycle HPC and the steam arrangement 200 as explained above- is suited to provide the flow of use steam US to the further heat exchanger W4.1 to heat the column sump in the further heat exchanger W4.1 of the fourth heat exchanging section W4.

[0320] In a way alternative options to use electrical energy or other heating device for heating the column sump become obsolete. Instead, the heat pump cycle HPC -with heat pump 100, and steam arrangement 200 as explained above with FIG. 2 coupled to the third exchanging section W3- is useful to extract heat from the third exchanging section W3 and provided to the further heat exchanging section W4 as shown in FIG. 4.

[0321] Referring to FIG. 5, therein an arrangement of steam compressors 220 is shown with the condenser CON. Respectively the arrangement comprises the condenser secondary side 210 as the steam generating unit and as part of the steam generating arrangement SGA. According to the description to FIG. 2 the steam generating arrangement SGA is adapted to transform the fresh steam FS of a basically undefined or not precisely definable input condition of input pressure and temperature pi, Ti to use steam US of a defined output condition of output pressure po and temperature To.

[0322] Herein, the arrangement of steam compressors 220 is provided with a first compressor stage C1 , a second compressor stage C2 and a third compressor stage C3. Each or selectively the compressors 220 in stages C1 , C2, C3 can be in a form of a screw compressor or a radial fan or an axial turbo compressor.

[0323] In particular, as shown schematically in FIG. 5, advantageously the fresh steam is sprayed off in at least one compressor stage C1 , C2, C3. In particular spraying is supported by a pump P to convey supply water SW in the steam generating arrangement SGA; the supply water SW here is used to spray water into at least one or some compressors (in this embodiment in compressor stages C2, C3) upstream of a compressor inlet. The pump P in this embodiment is provided as a pump P in aBASF SE

[0324]

[0325] 240181

[0326]

[0327] conduit or the like line for supply water SW in the steam generating arrangement SGA, wherein the pump P in the conduit or the like line for supply water SW in this embodiment is common to all compressor stages C1 , C2, C3. This arrangement has the advantage that in an adapted layout, the pump P can be sufficiently dimensioned as a single pump P common to the compressor stages C1 , 02, 03.

[0328] Also isolated solutions for screw compressors and centrifugal blowers exist, where water is sprayed in for cooling. It is generally advantageous (as long as a compressor allows it) to use injection cooling before a compressor stage (in this embodiment 02, 03) in order to set at least the suction-side temperature. If necessary also a temperature in a compressor of a compressor stage 02, 03 can be set by continuous evaporative cooling. Thus, preferably a minimum work effort or maximum COP can be achieved.

[0329] Still in the order of screw compressors, centrifugal fans, axial turbo compressors, the compressor blades become more sensitive to water droplets. In simple words, so to say, the blades of axial turbo compressors “should not see any water droplets”. Thus, water is usually added to “spray off” the steam after a compressor of a compressor stage with the longest possible inlet section. This measure is useful in order to avoid droplets on a compressor part, respectively to make sure that the spray water is evaporated fully at the inlet of a compressor of a compressor stage. Ideally, the water is sprayed to accelerate evaporation but also to avoid the formation of droplet streaks.

[0330] In a preferred embodiment, an injection takes place between two adjacent compressor stages (in this embodiment between stages 01 - 02 and between stages 02 - 03) to avoid an overheating of the compressed steam and to generate more steam by evaporating of the injected droplets.

[0331] In a preferred embodiment, all compressor stages are driven with electrical power from regenerative energy sources. In particular in this embodiment an electric motor M for driving a compressor of a compressor stage 01 , 02, 03 is driven with power generated from regenerative electrical energy sources like wind, solar or the like “green” energy sources. Also, in a preferred embodiment, all power consumptions explained above -namely the power consumption of the working fluid compressor 120 and of the steam compressor 220, more precisely the steam compressor arrangementBASF SE

[0332]

[0333] 240181

[0334]

[0335] COM- is generated “green”, i.e. the power is generated from regenerative electrical energy sources like wind, solar or the like “green” energy sources.

[0336] In summary a plant arrangement 1000 has been described hereinbefore with a method of production of ethylene oxide EO. The plant arrangement 1000 is adapted for the production of ethylene oxide EO, namely the plant arrangement is adapted to be operated according to the inventive concept of the process for producing ethylene oxide EO as has been described hereinbefore. The plant arrangement 1000 comprises a cycle gas arrangement 400 with a process reactor R1 , in particular a cycle gas loop with a process reactor.

[0337] Thus, in the plant arrangement 1000 for production of ethylene oxide EO:

[0338] (i) the process reactor R1 for producing ethylene oxide EO is adapted to receive at least ethylene and oxygen as parts of reactants,

[0339] (ii) the cycle gas arrangement is adapted to produce ethylene oxide EO by reacting the reactants including ethylene and oxygen in the presence of a catalyst in the process reactor R1 in a cycle gas stream and a cycle gas of the cycle gas stream at least comprises ethylene oxide EO,

[0340] (iii) the cycle gas arrangement has at least one heat exchanger W3.1 , in particular a heat exchanger W3.1 in form of a cooler, wherein the heat exchanger W3.1 is adapted to receive the cycle gas stream CGS, in particular with a primary side of the cooler,

[0341] (iv) the cycle gas arrangement 400 further has an ethylene oxide absorber column K1 , adapted to receive the cycle gas stream CGS and wash out ethylene oxide EO of the cycle gas CG applied to the ethylene oxide absorber column K1 with the cycle gas stream CGS,

[0342] (v) the cycle gas arrangement 400 has a carbon dioxide absorber column K2, adapted to receive the cycle gas stream CGS and wash out carbon dioxide CO2 of the cycle gas CG applied to the carbon dioxide absorber column K2 with the cycle gas stream CGS.

[0343] The plant arrangement is adapted to be operated according to the inventive concept of the process for producing ethylene oxide EO, wherein in the process :

[0344] (vi) the heat exchanger W3.1 is coupled in a water cooling cycle WCC adapted for cooling the cycle gas stream CGS by means of coolant water CW in the water cooling cycle WCC, in particular with a secondary side of the cooler, and

[0345] (vii) a water cooling arrangement 300 is provided with the water cooling cycle WCC, which is coupled to a heat pump cycle HPC of a heat pump 100 by providing the coolant water CW, as a heatBASF SE

[0346]

[0347] 240181

[0348]

[0349] source, to an evaporator EVA for a working fluid WF in the heat pump cycle HPC, and

[0350] (viii) a steam generator 200 with a steam generating arrangement SGA is coupled to the heat pump cycle HPC by providing supply water SW in the steam generating arrangement SGA, as a heat sink, to a condenser CON for the working fluid WF in the heat pump cycle HPC, wherein

[0351] (ix) the steam generating arrangement SGA is adapted for generating steam LS, US from the supply water SW.BASF SE

[0352]

[0353] 240181

[0354]

[0355] List of reference signs:

[0356] 100 heat pump, full cycle heat pump

[0357] 110 secondary side of evaporator EVA

[0358] 120 working fluid compressor

[0359] 130 condenser, primary side

[0360] 140 throttling valve

[0361] 200 steam arrangement

[0362] 210 condenser secondary side, supply water and steam side of the steam generating arrangement

[0363] 220 steam compressor, COM

[0364] 300 water cooling arrangement

[0365] 310 secondary side of heat exchanger W3.1

[0366] 320 primary side of evaporator EVA

[0367] 330 radiator

[0368] 340 pump

[0369] 400 cycle gas arrangement

[0370] 410 primary side of heat exchanger W3.1

[0371] 1000 plant arrangement

[0372] C1 first compressor stage

[0373] C2 second compressor stage

[0374] C3 third compressor stage

[0375] CG cycle gas

[0376] CGS cycle gas stream

[0377] CO2 carbon dioxideBASF SE

[0378]

[0379] 240181

[0380]

[0381] COM steam compressor arrangement

[0382] CON condenser

[0383] COP coefficient of performance

[0384] CW coolant water

[0385] EO ethylene oxide

[0386] EVA evaporator

[0387] HPC heat pump cycle

[0388] H2O supply water

[0389] K1 first absorption unit / column, ethylene oxide absorber column

[0390] K2 second absorption unit / column, carbon dioxide absorber column

[0391] K3 stripping column

[0392] LS, US live steam, use steam

[0393] P pump

[0394] P_el electrical power

[0395] R1 process reactor

[0396] SGA steam generating arrangement

[0397] SW supply water, VE water

[0398] W1 first heat exchanging section

[0399] W1.1 first heat exchanger in the form of a steam generator

[0400] W2 second heat exchanging section

[0401] W2.1 second heat exchanger in the form of a “gas-to-gas” - recuperator

[0402] W3 third heat exchanging section

[0403] W3.1 heat exchanger in the form of a cooler

[0404] W4 fourth heat exchanging section| BASF SE

[0405]

[0406] | 240181

[0407]

[0408] W4.1 heat exchanger

[0409] WCC water cooling cycle

[0410] WF working fluid

[0411] Q1 , Q2, Q3 heat

[0412] p pressure

[0413] T Temperature

Claims

BASF SE240181CLAIMS1. Method of production of ethylene oxide (EO), wherein in a process for producing ethylene oxide (EO):(i) at least ethylene and oxygen is provided as parts of reactants to a process reactor (R1) for producing ethylene oxide (EO),(ii) ethylene oxide (EO) is produced by reacting the reactants including ethylene and oxygen in the presence of a catalyst in the process reactor (R1) in a cycle gas stream (CGS) and a cycle gas (CG) of the cycle gas stream (CGS) at least comprises ethylene oxide (EO),(iii) the cycle gas stream (CGS) is provided to a heat exchanger (W3.1), in particular a heat exchanger (W3.1) in form of a cooler,(iv) ethylene oxide (EO) is washed out of the cycle gas (CG) by applying the cycle gas stream (CGS) to an ethylene oxide absorber column (K1),(v) carbon dioxide (CO2) is washed out of the cycle gas (CG) by applying the cycle gas stream (CGS) to a carbon dioxide absorber column (K2),- wherein in the process :(vi) the heat exchanger (W3.1) is coupled in a water cooling cycle adapted for cooling the cycle gas stream (CGS) by means of coolant water (CW) of the water cooling cycle (WCC), and(vii) the water cooling cycle (WCC) is coupled to a heat pump cycle (HPC) by providing the coolant water (CW) as a heat source to an evaporator (EVA) adapted for a working fluid (WF) in the heat pump cycle (HPC), and(viii) a steam generating arrangement (SGA) is coupled to the heat pump cycle (HPC) by providing supply water (SW) in the steam generating arrangement (SGA), as a heat sink, to a condenser (CON) for the working fluid (WF) in the heat pump cycle (HPC), wherein(ix) the steam generating arrangement (SGA) is adapted for generating steam (LS, US) from the supply water (SW).

2. Method of claim 1 , wherein the cycle gas stream is provided to the heat exchanger (W3.1) in form of the cooler in said exchanging section and the cycle gas stream is provided to a further heat exchanger (W1.1 , W2.1) in a further heat exchanging section (W1 , W2) upstream of said heat exchanger in said exchanging section.BASF SE2401813. Method of claim 2, wherein said first heat exchanging section comprises at least said further heat exchanger (W1.1 , W2.1) in form of a steam generator and / or a still further heat exchanger in form of a “gas-to-gas”- recuperator.

4. Method of any of the preceding claims, wherein the water cooling cycle (WCC) is operated in a predetermined temperature range, wherein the heat exchanger (W3.1) in form of the cooler is part of the water cooling cycle (WCC) and is formed as a liquid / liquid heat exchanger operated on the cycle gas (CG) at a primary side temperature in temperature range of 40°C to 90°C and operated on the coolant water (CW) at a secondary side temperature in a temperature range of 45° C to 66° C.

5. Method of any of the preceding claims, wherein the steam generating arrangement comprises- a first steam generating unit, in particular a condenser secondary side of condenser of the heat pump cycle (HPC), for generating fresh steam (FS) from the supply water (SW), and- a second steam generating unit, for compressing the fresh steam (FS) to use-steam of a specified pressure (p) and temperature (T).

6. Method of any of the preceding claims, wherein the working fluid is a refrigerant selected from the group consisting of butane, in particular n-butane or iso-butane, and ammonia.

7. Method of any of the preceding claims, wherein the heat pump cycle is operated at a COP in the range from 2.5 to 3.5.

8. Method of any of the preceding claims, wherein- supply water (SW) supplied to the steam generating arrangement is demineralized and / or degassed water (VE), and / or- the use-steam is adapted to be used as grid-steam, plant / process-steam or turbine steam, and / or - electric power for working fluid compressor and / or steam compressor is generated from a regenerative energy source.BASF SE2401819. Plant arrangement (1000) adapted for the production of ethylene oxide (EO), in particular wherein the plant arrangement (1000) is adapted to operate the method as claimed in any of the preceding claims, the plant arrangement (1000) comprising a cycle gas arrangement (400) with a process reactor (R1), in particular a cycle gas loop with a process reactor, wherein in the plant arrangement (1000) for production of ethylene oxide (EO),(i) the process reactor (R1) for producing ethylene oxide (EO) is adapted to receive at least ethylene and oxygen as parts of reactants,(ii) the cycle gas arrangement is adapted to produce ethylene oxide (EO) by reacting the reactants including ethylene and oxygen in the presence of a catalyst in the process reactor (R1) in a cycle gas stream and a cycle gas of the cycle gas stream at least comprises ethylene oxide (EO), (iii) the cycle gas arrangement has at least one heat exchanger (W3.1), in particular a heat exchanger (W3.1) in form of a cooler, wherein the heat exchanger (W3.1) is adapted to receive the cycle gas stream (CGS), in particular with a primary side of the cooler,(iv) the cycle gas arrangement (400) further has an ethylene oxide absorber column (K1), adapted to receive the cycle gas stream (CGS) and wash out ethylene oxide (EO) of the cycle gas (CG) applied to the ethylene oxide absorber column (K1) with the cycle gas stream (CGS),(v) the cycle gas arrangement (400) has a carbon dioxide absorber column (K2), adapted to receive the cycle gas stream (CGS) and wash out carbon dioxide (CO2) of the cycle gas (CG) applied to the carbon dioxide absorber column (K2) with the cycle gas stream (CGS),wherein in the process :(vi) the heat exchanger (W3.1) is coupled in a water cooling cycle (WCC) adapted for cooling the cycle gas stream (CGS) by means of coolant water (CW) in the water cooling cycle (WCC), in particular with a secondary side of the cooler, and(vii) a water cooling arrangement (300) is provided with the water cooling cycle (WCC), which is coupled to a heat pump cycle (HPC) of a heat pump (100) by providing the coolant water (CW), as a heat source, to an evaporator (EVA) for a working fluid (WF) in the heat pump cycle (HPC), and (viii) a steam generator (200) with a steam generating arrangement (SGA) is coupled to the heat pump cycle (HPC) by providing supply water (SW) in the steam generating arrangement (SGA), as a heat sink, to a condenser (CON) for the working fluid (WF) in the heat pump cycle (HPC), wherein(ix) the steam generating arrangement (SGA) is adapted for generating steam (LS, US) from the supply water (SW).BASF SE24018110. Plant arrangement (1000) of claim 9, whereinthe steam generating arrangement (SGA) of the steam generator (200) comprises the condenser (CON),- said condenser (CON), in particular with a secondary side of condenser, being adapted as a first steam generating unit for generating fresh steam from the supply water (SW), andthe steam generating arrangement (SGA) comprises a steam compressor,- said steam compressor (220, COM) being adapted for compressing the fresh steam (FS) to usesteam (US) of a specific pressure and temperature.

11. Plant arrangement (1000) of claim 9 or 10, wherein- the heat pump cycle (HPC) has a working fluid compressor (120) formed as a turbo compressor, in particular in form of a hermetic and / or single shaft turbo compressor, in particular in the case the working fluid is a refrigerant in form of butane, and / or- the heat pump cycle has a working fluid compressor (120) formed as a piston compressor, in particular in form of a hermetic piston compressor, in particular in the case the working fluid is a refrigerant in form of Ammonia.

12. Plant arrangement (1000) of any of the claims 9 to 11 , wherein the water cooling cycle (WCC) comprises the heat exchanger in the form of the cooler, in particular with the secondary side (310) of the cooler, an air radiator, a pump and the evaporator (EVA) of the heat pump cycle (HPC), in particular with a primary side (320) of evaporator (EVA).

13. Plant arrangement (1000) of any of the claims 9 to 12, wherein the heat pump cycle has the evaporator, in particular with the secondary side of evaporator, a working fluid compressor, the condenser, in particular with the primary side of condenser, and a throttle vent.

14. Plant arrangement (1000) of any of the claims 9 to 13, wherein a secondary side of evaporator, namely a heat source side of the evaporator, is formed as a flash evaporator wherein the refrigerant is evaporated by means of a forced-circulation flash evaporation or a falling film evaporator wherein the refrigerant is evaporated by means of a falling-film evaporation.| BASF SE24018115. Plant arrangement (1000) of any of the claims 9 to 14, wherein a secondary side of condenser, namely a heat sink side of the condenser, is formed as a falling-film evaporator, wherein the supply water is evaporated by means of a falling-film evaporation.

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