Carbon dioxide capture and storage in industrial chemical processes

Abstract

The invention relates to a method and a device for purifying a gas stream comprising 30.0 mol% to 99.8 mol% of carbon dioxide and 0.1 mol% to 60.0 mol% of water, and the use of the process or apparatus for purifying a carbon dioxide stream originating from an industrial chemical process and using the purified carbon dioxide stream as a feed stream in further industrial chemical processes or in beverage production or carbon capture storage.

Description

[0001] The present invention relates to a method and apparatus for purifying a gas stream comprising 30.0 mol% to 99.8 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water, and the use of said method or apparatus for purifying a carbon dioxide stream derived from an industrial chemical process and using said purified carbon dioxide stream as a feed stream in a further industrial chemical process or in beverage production or carbon capture and storage. Background Technology

[0002] Industrial chemical processes are sources of byproduct streams containing carbon dioxide, which, when released into the environment, can have a significant impact on climate change. Exemplary industrial chemical processes with considerably high levels of carbon dioxide byproduct streams are methods used to produce basic chemicals, such as ethylene oxide or ammonia.

[0003] Carbon dioxide can be recycled and used as a feed stream for other industrial chemical processes or for other purposes, such as liquefied carbon dioxide used in the food industry. For such recycling applications, the byproduct stream needs to be purified. Water removal is particularly important.

[0004] Suitable materials for removing water from a gas stream include, for example, silicates or aluminum silicates or activated alumina or molecular sieves.

[0005] For each of these adsorbents used to remove water, the method for purifying the carbon dioxide-containing stream needs to be optimized, especially based on potential contaminants that could poison the chosen water adsorbent. Such contaminants include, for example, oxygen and ethylene.

[0006] This invention provides a method and apparatus for purifying a gas stream containing 30.0 mol% to 99.8 mol% carbon dioxide and 0.1 mol% to 30.0 mol% water, the gas stream further containing one or both of the following: 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 1000 mol-ppm, preferably 25 mol-ppm to 750 mol-ppm, more preferably 50 mol-ppm to 500 mol-ppm ethylene. It has been found that oxygen and / or ethylene can be removed from the gas stream by subjecting it to a hydrogenation step in the presence of a metal catalyst, thus preventing the oxygen and / or ethylene from poisoning the adsorbent in the water adsorption unit during downstream process steps for water adsorption.

[0007] The method and apparatus have been optimized to obtain a purified stream with a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%, which can be recycled and used as a feed stream for other industrial chemical processes or for other purposes, such as liquefied carbon dioxide used in the food industry, or can be stored in a carbon capture and storage device. Summary of the Invention

[0008] In a first aspect, the present invention relates to a method for purifying a stream of carbon dioxide, the method comprising the following steps:

[0009] • Provide a gas stream comprising 30.0 mol% to 99.8 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water, and additionally comprising one or both of 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene;

[0010] • In the presence of a metal catalyst, a gas stream is subjected to a hydrogenation step for removing oxygen and / or ethylene from the gas stream. The metal catalyst is preferably a catalyst containing platinum, palladium and / or ruthenium, more preferably a catalyst containing platinum or palladium, and is preferably supported by a support material.

[0011] • Subject the gas stream to one or more compression steps to obtain a compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg;

[0012] • The compressed gas stream is cooled downstream of the hydrogenation step and one or more compression steps to obtain a cooled compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C.

[0013] • Water is adsorbed from a cooled compressed gas stream in a water adsorption unit to obtain a dry gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 100 ppm-mol, preferably 0 ppm-mol to 50 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

[0014] In a second aspect, the present invention relates to an apparatus for purifying a stream of carbon dioxide, the apparatus comprising:

[0015] • A component for reducing the amount of oxygen and / or ethylene in a gas stream, preferably a component for hydrogenating oxygen and / or ethylene, more preferably a hydrogenator, wherein the component for reducing the amount of oxygen and / or ethylene in a gas stream comprises a metal catalyst, preferably a catalyst comprising platinum, palladium and / or ruthenium, more preferably a catalyst comprising platinum or palladium, and preferably supported by a support material.

[0016] • One or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components connected in series for compressing a gas stream, preferably a compressor, wherein the gas stream comprises 30.0 mol% to 99.8 mol% carbon dioxide, 0.1 mol% to 60.0 mol% water, and additionally comprises 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene, or both;

[0017] • In one or more components for compressing a gas stream, preferably downstream of a compressor, components for cooling the compressed gas stream;

[0018] • A water adsorption unit downstream of a component used for cooling a compressed gas stream, for adsorbing water from the cooled compressed gas stream; and

[0019] • A component used to transport a stream of cooled compressed gas from a component used to cool the compressed gas stream to a water adsorption unit.

[0020] In a third aspect, the present invention relates to the use of the methods and / or apparatus described above or below for purifying a carbon dioxide stream derived from an industrial chemical process, preferably from a process for producing ethylene oxide, and for using the purified carbon dioxide stream as a feed stream in a further industrial chemical process or in beverage production or carbon capture and storage. Attached Figure Description

[0021] Figure 1 A schematic overview of the method and apparatus of the present invention for purifying a carbon dioxide-containing stream originating from a method for producing ethylene oxide is shown.

[0022] Figure 2 A schematic overview of the method and apparatus of the present invention for purifying carbon dioxide-containing streams originating from a process for producing ethylene oxide and another carbon dioxide-containing stream originating from a process for producing ammonia, is shown, the streams being combined in a water adsorption unit.

[0023] Figure 3 A schematic overview of a preferred embodiment of a water adsorption unit having three sub-units arranged in parallel is shown, wherein two sub-units operate in working mode and one sub-unit operates in regeneration mode. Detailed Implementation

[0024] method

[0025] In a first aspect, the present invention relates to a method for purifying a stream of carbon dioxide, the method comprising the following steps:

[0026] • Provide a gas stream comprising 30.0 mol% to 99.8 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water, and additionally comprising one or both of 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene;

[0027] • In the presence of a metal catalyst, a gas stream is subjected to a hydrogenation step for removing oxygen and / or ethylene from the gas stream. The metal catalyst is preferably a catalyst containing platinum, palladium and / or ruthenium, more preferably a catalyst containing platinum or palladium, and is preferably supported by a support material.

[0028] • Subject the gas stream to one or more compression steps to obtain a compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg;

[0029] • The compressed gas stream is cooled downstream of the hydrogenation step and one or more compression steps to obtain a cooled compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C.

[0030] • Water is adsorbed from a cooled compressed gas stream in a water adsorption unit to obtain a dry gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 100 ppm-mol, preferably 0 ppm-mol to 50 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

[0031] The method of the first aspect of the invention as described above or below is preferably adapted to operate in the apparatus of the second aspect of the invention as described above or below.

[0032] The gas flow preferably has a pressure of 0.001 barg to 0.50 barg, more preferably 0.002 barg to 0.20 barg, and even more preferably 0.005 barg to 0.10 barg.

[0033] Furthermore, the gas flow preferably has a temperature of 25°C to 65°C, more preferably 30°C to 60°C, and even more preferably 40°C to 55°C.

[0034] The gas stream preferably originates from industrial chemical processes, more preferably from industrial processes for producing one or more basic chemicals, such as processes for producing ethylene oxide and / or ethylene glycol.

[0035] The carbon dioxide content of the gas stream is 30.0 mol% to 99.8 mol%, preferably 50.0 mol% to 99.0 mol%, and more preferably 75.0 mol% to 98.0 mol%.

[0036] In addition, the water content of the gas stream is 0.1 mol% to 60.0 mol%, preferably 0.5 mol% to 40.0 mol%, and more preferably 1.0 mol% to 20.0 mol%.

[0037] Furthermore, the gas stream contains one or both of oxygen and / or ethylene. Ethylene and oxygen may be included in the gas stream as unreacted segregants, which originates from industrial processes used to produce one or more basic chemicals, such as those used to produce ethylene oxide and / or ethylene glycol.

[0038] If present, the oxygen content of the gas stream is 25 mol-ppm to 10,000 mol-ppm, preferably 50 mol-ppm to 7,500 mol-ppm, and more preferably 100 mol-ppm to 5,000 mol-ppm.

[0039] If present, the ethylene content of the gas stream is 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, and more preferably 50 mol-ppm to 1500 mol-ppm ethylene.

[0040] The gas stream may contain up to 40 mol% of gaseous components that are different from carbon dioxide, water, oxygen and ethylene.

[0041] The contents of carbon dioxide, water, oxygen, ethylene, and gaseous components different from carbon dioxide, water, oxygen, or ethylene typically constitute 100 mol of the split gas stream.

[0042] The total mass flow rate of the gas stream is preferably in the range of 2,500 kg / h to 150,000 kg / h, more preferably 3,000 kg / h to 135,000 kg / h, and more preferably 5,000 kg / h to 125,000 kg / h.

[0043] The mass flow rate of a gas stream typically depends on the industrial chemical process from which it originates.

[0044] When derived from a method for producing ethylene oxide and / or ethylene glycol, the total mass flow rate is typically in the range of 2,500 kg / h to 60,000 kg / h, preferably 3,000 kg / h to 50,000 kg / h, and more preferably 5,000 kg / h to 45,000 kg / h.

[0045] The gas stream is subjected to one or more compression steps to obtain a compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, and more preferably 30 barg to 45 barg.

[0046] Typically, a gas stream is subjected to two to ten compression steps, preferably three to eight compression steps, and more preferably five to six compression steps to obtain a compressed gas stream.

[0047] The compression step preferably increases the pressure of the gas flow by 0.1 bar to 10 bar, more preferably 0.2 bar to 7.5 bar, and more preferably 0.5 bar to 5.0 bar in each compression step.

[0048] The compression step is preferably optimized for the mass flow rate of the gas stream at a gas flow rate of 2,500 kg / h to 85,000 kg / h, preferably 3,000 kg / h to 80,000 kg / h, and more preferably 5,000 kg / h to 75,000 kg / h.

[0049] Therefore, for gas flows with a mass flow rate exceeding 75,000 kg / h, 80,000 kg / h, or 85,000 kg / h, there is a possibility that the excess gas flow may be diverted after the first compression step.

[0050] The diverted gas stream can be used as a low-pressure gas stream containing carbon dioxide for other industrial purposes.

[0051] The diverted gas flow preferably has a pressure of 0.1 barg to 1.5 barg, more preferably 0.2 barg to 1.2 barg, and even more preferably 0.5 barg to 1.0 barg.

[0052] Furthermore, the diverted gas flow preferably has a temperature of 20°C to 50°C, more preferably 25°C to 45°C, and even more preferably 30°C to 40°C.

[0053] Furthermore, the split gas stream preferably has a carbon dioxide content of 30.0 mol% to 99.8 mol%, more preferably 50.0 mol% to 99.0 mol%, and even more preferably 75.0 mol% to 98.0 mol%.

[0054] Furthermore, the split gas stream preferably has a water content of 0.1 mol% to 30.0 mol%, preferably 0.5 mol% to 20.0 mol%, and more preferably 1.0 mol% to 15.0 mol%.

[0055] In addition, the split gas stream preferably contains one or both of the following: 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 1000 mol-ppm, preferably 25 mol-ppm to 750 mol-ppm, more preferably 50 mol-ppm to 500 mol-ppm ethylene.

[0056] The split gas stream may contain up to 40 mol% of gaseous components that are different from carbon dioxide, water, oxygen or ethylene.

[0057] The contents of carbon dioxide, water, oxygen, ethylene, and gaseous components different from carbon dioxide, water, oxygen, or ethylene typically constitute 100 mol of the split gas stream.

[0058] Downstream of the final compression step, a compressed gas stream with a pressure of 25 barg to 50 barg, preferably 30 barg to 45 barg, is obtained.

[0059] Typically, the temperature of the gas stream increases during each compression step due to the energy introduced during the compression step.

[0060] The temperature of the compressed gas stream is preferably 75°C to 150°C, more preferably 85°C to 140°C, and even more preferably 90°C to 125°C.

[0061] The compressed gas stream is cooled to obtain a cooled compressed gas stream having a pressure of 25 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C.

[0062] The cooling step may be performed in a single cooling step downstream of one or more compression steps.

[0063] Alternatively, downstream of the hydrogenation step and each compression step, the gas stream is cooled to a temperature of 25°C to 55°C, preferably 30°C to 50°C, and more preferably 35°C to 45°C.

[0064] The cooled compressed gas stream is subjected to a water adsorption step, as discussed in detail below. Thus, water is adsorbed from the cooled compressed gas stream in the water adsorption unit to obtain a dry gas stream.

[0065] Ethylene and oxygen present in the gas stream are considered toxic to the adsorbent in the water adsorbent unit, i.e., they may deactivate the adsorbent. Therefore, the method of the present invention provides a method step upstream of the water adsorption step for removing oxygen and / or ethylene from the gas stream.

[0066] Oxygen and / or ethylene are removed from a gas stream by hydrogenation in the presence of a metal catalyst, preferably a catalyst containing platinum, palladium and / or ruthenium, more preferably platinum or palladium.

[0067] Metal catalysts are preferably suitable for converting oxygen to water in the presence of hydrogen, and for converting ethylene to ethane in the presence of hydrogen.

[0068] Metal catalysts are preferably supported by a carrier material.

[0069] The carrier material is preferably alumina (Al2O3) or silicon dioxide (SiO2), and preferably sintered alumina.

[0070] Suitable carrier materials include, for example, tablet carriers, extrusions, spheres, and coated monolithic catalysts.

[0071] The tablet carrier preferably has a size of 1 mm × 1 mm to 5 mm × 5 mm, more preferably 2 mm × 2 mm to 4 mm × 4 mm (such as about 3 mm × 3 mm).

[0072] The spherical carrier preferably has an average particle size of 1 mm to 10 mm, more preferably 2 mm to 8 mm (such as 2 mm to 4 mm or about 8 mm).

[0073] Carrier materials are commercially available. Suitable carrier materials are, for example, those named CSS and SAS, such as CSS 350 or SAS 90, which are commercially available from BASF SE.

[0074] Based on the total weight of the metal catalyst and the support material, the metal catalyst is preferably present on the support material in an amount of 0.01% to 1.0% by weight, more preferably 0.02% to 0.7% by weight, and even more preferably 0.05% to 0.5% by weight.

[0075] Metal catalysts can be introduced onto the support material through impregnation.

[0076] Metal catalysts are commercially available. A suitable metal catalyst is, for example, PuriStar, which is commercially available from BASF SE. ® R0-20 or more specifically R0-20 / 25.

[0077] Prior to hydrogenation, the gas stream is preferably compressed to a pressure of 3 barg to 12 barg, more preferably 5 barg to 10 barg, and even more preferably 6 barg to 8 barg.

[0078] Preferably, a gas stream with a pressure of 3 barg to 12 barg, more preferably 5 barg to 10 barg, and even more preferably 6 barg to 8 barg is directed from one or more compression steps, preferably two to ten compression steps, and more preferably three to eight compression steps (such as five to six compression steps) to a hydrogenation step to obtain a compressed gas stream with a pressure of 25 barg to 50 barg, preferably 30 barg to 45 barg.

[0079] Typically, in such a cascade of one or more compression steps, preferably two to ten compression steps, more preferably three to eight compression steps (such as five to six compression steps), a gas flow at a pressure of 3 to 12 barg, more preferably 5 to 10 barg, and even more preferably 6 to 8 barg is directed to a hydrogenation step downstream of the second to eighth compression steps, preferably the third or fourth compression step.

[0080] Prior to the hydrogenation step, the gas stream preferably has a temperature of 130°C to 180°C, more preferably 140°C to 175°C, and even more preferably 150°C to 170°C. To achieve this temperature range, the gas stream is preferably heated prior to the hydrogenation step.

[0081] In the hydrogenation step, the gas stream is passed through a stream containing 99.0 mol% to 100 mol% hydrogen.

[0082] The flow containing 99.0 mol% to 100 mol% hydrogen preferably has a pressure of 3 barg to 12 barg, more preferably 5 barg to 10 barg, and even more preferably 6 barg to 9 barg.

[0083] Furthermore, the stream containing 99.0 mol% to 100 mol% hydrogen preferably has a temperature of 10°C to 45°C, more preferably 12°C to 40°C.

[0084] Preferably, the stream containing 99.0 mol% to 100 mol% hydrogen has a pressure 0.1 barg to 1.0 barg, preferably 0.2 barg to 0.5 barg higher than the compressed gas stream before hydrogenation.

[0085] Preferably, the mass flow rate of the stream containing 99.0 mol% to 100 mol% hydrogen is adjusted to a stoichiometric amount of hydrogen relative to the amount of oxygen and ethylene present in the gas stream.

[0086] Typically, the mass flow rate of the stream containing 99.0 mol% to 100 mol% hydrogen is in the range of 0.1 kg / h to 25.0 kg / h, preferably 0.2 kg / h to 20.0 kg / h, and more preferably 0.5 kg / h to 15.0 kg / h.

[0087] The stream containing 99.0 mol% to 100 mol% hydrogen is preferably contacted with the gas stream in the presence of a metal catalyst, such that oxygen is hydrogenated to water and ethylene is hydrogenated to ethane.

[0088] Following the hydrogenation step, the gas stream preferably has a low content of oxygen and / or ethylene.

[0089] After the hydrogenation step, the gas stream preferably has an oxygen content of less than 100 ppm-mol, preferably from 0 ppm-mol to 50 ppm-mol.

[0090] Furthermore, after the hydrogenation step, the gas stream preferably has an ethylene content of less than 10 ppm-mol, preferably from 0 ppm-mol to 7.5 ppm-mol.

[0091] After the hydrogenation step, the gas stream preferably has a pressure of 3 barg to 12 barg, more preferably 5 barg to 10 barg, and even more preferably 6 barg to 8 barg.

[0092] Furthermore, after hydrogenation, the gas stream preferably has a temperature of 130°C to 190°C, more preferably 140°C to 180°C, and even more preferably 155°C to 175°C.

[0093] Preferably, the gas stream following the hydrogenation step is further compressed to obtain a compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, and more preferably 30 barg to 45 barg. Thus, the gas stream following the hydrogenation step is preferably redirected to a cascade of one or more, preferably two to ten, and more preferably three to eight compression steps.

[0094] Therefore, downstream of the hydrogenation step and upstream of the further compression step, the gas flow preferably has a temperature of 75°C to 150°C, more preferably 85°C to 140°C, and more preferably 90°C to 125°C. To achieve this temperature range, the gas flow can be cooled downstream of the hydrogenation step and upstream of the further compression step.

[0095] Downstream of the compression step, a cooled compressed gas stream is passed through a water adsorption step. This cooled compressed gas stream has a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C. Thus, water is adsorbed from the cooled compressed gas stream in the water adsorption unit to obtain a dry gas stream.

[0096] Water adsorption units typically contain an adsorbent for removing water. A suitable adsorbent is aluminosilicate.

[0097] Based on the total weight of the aluminosilicate, the aluminosilicate preferably has an alumina (Al2O3) content of 1.0 wt% to 7.5 wt%, more preferably 2.0 wt% to 6.0 wt%, and even more preferably 2.5 wt% to 5.0 wt%.

[0098] Furthermore, based on the total weight of the aluminosilicate, the aluminosilicate preferably has a silicon dioxide (SiO2) content of 92.5% to 99.0% by weight, more preferably 94.0% to 98.0% by weight, and even more preferably 95.0% to 97.5% by weight.

[0099] Preferably, the aluminosilicate is composed of aluminum oxide and silicon dioxide.

[0100] Aluminosilicates are preferably present in the water adsorption unit in the form of gel, and more preferably in the form of gel beads.

[0101] Aluminosilicates preferably have a surface area of ​​500 m² / g to 850 m² / g, more preferably 550 m² / g to 800 m² / g, and even more preferably 600 m² / g to 775 m² / g.

[0102] Furthermore, the aluminosilicate preferably has a pore volume of 0.30 ml / g to 0.55 ml / g, more preferably 0.35 ml / g to 0.50 ml / g, and even more preferably 0.40 ml / g to 0.46 ml / g.

[0103] Furthermore, the pressure dew point of the gas flow around the aluminosilicate is preferably in the range of -50°C to -75°C, more preferably -55°C to -70°C, and even more preferably -57°C to -67°C.

[0104] Furthermore, the desorption temperature of aluminosilicate is preferably in the range of 100°C to 175°C, more preferably 110°C to 165°C, and even more preferably 115°C to 155°C.

[0105] Aluminosilicates are commercially available. Suitable aluminosilicates can be found under the trade name Sorbead. ®(Preferably Sorbead) ® The Air was purchased from BASF SE.

[0106] During the water adsorption step, water is adsorbed by aluminosilicate. To improve the water adsorption capacity and thus the efficiency of the water adsorption step, it is preferable to desorb the adsorbed water from the aluminosilicate from time to time so as to regenerate the aluminosilicate in the regeneration step.

[0107] The adsorbent is preferably regenerated by contact with a gas stream having an elevated temperature. Preferably, the regeneration stream has a temperature in the range of 100°C to 175°C, more preferably 110°C to 165°C, and even more preferably 115°C to 155°C.

[0108] Typically, for commercially available adsorbents, the preferred desorption temperature is disclosed in the technical data provided by the distributor.

[0109] During regeneration mode, adsorbed water is removed from the adsorbent through temperature-switching adsorption. Thus, water desorbs from the adsorbent at elevated temperatures.

[0110] The regeneration stream can be any gas stream available at elevated temperatures.

[0111] Preferably, the regeneration stream is split upstream of the cooling step with a compressed gas stream at a pressure of 25 barg to 50 barg, preferably 30 barg to 45 barg.

[0112] Upstream of the cooling step, the compressed gas stream typically has a temperature of 75°C to 150°C, preferably 85°C to 140°C, and more preferably 90°C to 125°C.

[0113] If the temperature of the compressed gas stream upstream of the cooling step is within the preferred desorption temperature range of the adsorbent, the heat exchange step of the regeneration stream can be omitted.

[0114] Alternatively, the compressed gas stream diverted from the cooling step can be passed through a heat exchange step so that the temperature of the diverted compressed gas stream reaches the preferred desorption temperature range of the adsorbent.

[0115] To increase the rate of water desorption from the adsorbent, the pressure of the cooling compressed gas stream can be reduced by 0.5 bar to 2.5 bar, preferably 0.7 bar to 1.5 bar, and more preferably 1 bar.

[0116] Downstream of the water adsorption unit, the regeneration gas is preferably recycled by redirecting the regeneration gas containing water desorbed from the adsorbent during the regeneration mode into a compressed gas stream upstream of the water adsorption step.

[0117] The regenerated gas is preferably cooled before being redirected into the compressed gas stream, and the desorbed water is preferably separated from the cooled regenerated gas.

[0118] The regeneration step can be performed during the downtime of the method of the present invention. In the embodiment described, a single water adsorption unit preferably comprising aluminosilicate as an adsorbent is sufficient for the water adsorption step.

[0119] However, preferably, the regeneration step is performed during the method of the present invention. In the described embodiment, the water adsorption unit preferably comprises at least two sub-units, more preferably two to five sub-units, and even more preferably three sub-units. The two or more sub-units are preferably arranged in parallel.

[0120] Thus, at least one sub-unit is in operating mode, in which water is adsorbed from the cooling compressed gas stream, and at least one sub-unit is in regeneration mode, in which the adsorbed water is removed from the adsorbent.

[0121] In a particularly preferred embodiment, the water adsorption unit comprises three sub-units, two of which are in operating mode and one sub-unit is in regeneration mode. Thus, each sub-unit preferably remains in operating mode for two-thirds of the time increment of the method of the invention and in regeneration mode for one-third of the time increment.

[0122] The total mass flow rate of the drying gas stream is in the range of 2,000 kg / h to 175,000 kg / h, preferably 2,500 kg / h to 165,000 kg / h, and more preferably 4,500 kg / h to 155,000 kg / h.

[0123] In a first embodiment where the gas stream originates from a method for producing ethylene oxide and / or ethylene glycol, the total mass flow rate of the drying gas stream is in the range of 2,000 kg / h to 60,000 kg / h, preferably 2,500 kg / h to 50,000 kg / h, and more preferably 4,500 kg / h to 45,000 kg / h.

[0124] In the second embodiment, the gas stream may originate from more than one industrial chemical process, such as a process for producing ethylene oxide and / or ethylene glycol and a process for producing ammonia.

[0125] In the described embodiments, gas streams originating from two or more industrial processes typically differ in their composition, particularly in terms of potentially toxic components, such that not all gas streams originating from two or more industrial processes require a hydrogenation step. Gas streams originating from two or more industrial processes may also differ in their temperature and / or pressure, necessitating different amounts of compression steps and different temperature conditions.

[0126] Therefore, gas streams derived from two or more industrial methods are preferably processed separately in a compression step, a cooling step, and optionally a hydrogenation step to obtain a compressed and cooled compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C.

[0127] Preferably, upstream of the water adsorption step in the water adsorption unit, different gas streams are combined into a combined compressed, cooled compressed gas stream.

[0128] Exemplary gas streams derived from methods for producing ammonia typically do not contain significant amounts of components considered toxic to adsorbents (i.e., capable of deactivating them), such as oxygen and / or ethylene. Therefore, a hydrogenation step is generally not required for gas streams derived from methods for producing ammonia.

[0129] In the second embodiment, the method preferably further includes the following steps:

[0130] A second gas stream is provided, the second gas stream comprising preferably 40.0 mol% to 99.9 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water;

[0131] The second gas stream is subjected to one or more compression steps to obtain a compressed second gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg;

[0132] Downstream of the hydrogenation step and one or more compression steps, the compressed second gas stream is cooled to obtain a cooled compressed second gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, preferably 30 barg to 45 barg and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C.

[0133] Combining the cooled compressed second gas stream and the cooled compressed gas stream to obtain a combined cooled compressed gas stream; and

[0134] In a water adsorption unit, water is adsorbed from a combined cooled compressed gas stream to obtain a dry combined gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 25 ppm-mol, preferably 0 ppm-mol to 20 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

[0135] The second gas stream preferably originates from a method for producing ammonia.

[0136] The carbon dioxide content of the second gas stream is preferably 40.0 mol% to 99.9 mol%, preferably 60.0 mol% to 99.5 mol%, and more preferably 80.0 mol% to 99.0 mol%.

[0137] In addition, the water content of the second gas stream is 0.1 mol% to 60.0 mol%, preferably 0.5 mol% to 40.0 mol%, and more preferably 1.0 mol% to 20.0 mol%.

[0138] The second gas stream may contain up to 2.5 mol% of gaseous components that are different from carbon dioxide or water.

[0139] The contents of carbon dioxide, water, and gaseous components different from carbon dioxide or water typically constitute 100 mol of the second gas stream.

[0140] Preferably, the total mass flow rate of the second gas stream is in the range of 50,000 kg / h to 150,000 kg / h, more preferably 65,000 kg / h to 135,000 kg / h, and more preferably 70,000 kg / h to 125,000 kg / h.

[0141] The second gas stream is subjected to one or more compression steps to obtain a compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg.

[0142] Typically, the second gas stream is subjected to two to ten compression steps, preferably three to eight compression steps, and more preferably five to six compression steps to obtain a compressed second gas stream.

[0143] The compression step preferably increases the pressure of the second gas stream by 0.1 bar to 10 bar, more preferably 0.2 bar to 7.5 bar, and more preferably 0.5 bar to 5.0 bar in each compression step.

[0144] The compression step is preferably optimized for the mass flow rate of the second gas stream at 50,000 kg / h to 120,000 kg / h, preferably 65,000 kg / h to 110,000 kg / h, and more preferably 70,000 kg / h to 100,000 kg / h.

[0145] Therefore, for a second gas flow with a mass flow rate exceeding 100,000 kg / h, 110,000 kg / h, or 120,000 kg / h, there is a possibility that the excess second gas flow may be diverted after the first compression step.

[0146] The split second gas stream can be used as a low-pressure second gas stream containing carbon dioxide for other industrial purposes.

[0147] The second gas stream of the diversion preferably has a pressure of 0.1 barg to 1.5 barg, more preferably 0.2 barg to 1.2 barg, and even more preferably 0.5 barg to 1.0 barg.

[0148] Furthermore, the second gas stream in the split preferably has a temperature of 20°C to 50°C, more preferably 25°C to 45°C, and even more preferably 30°C to 40°C.

[0149] Furthermore, the second gas stream in the split preferably has a carbon dioxide content of 40.0 mol% to 99.9 mol%, more preferably 60.0 mol% to 99.5 mol%, and even more preferably 80.0 mol% to 99.0 mol%.

[0150] Furthermore, the second gas stream in the split preferably has a water content of 0.1 mol% to 60.0 mol%, preferably 0.5 mol% to 40.0 mol%, and more preferably 1.0 mol% to 20.0 mol%.

[0151] The split gas stream may contain up to 2.5 mol% of gaseous components that are different from carbon dioxide, water, oxygen or ethylene.

[0152] The contents of carbon dioxide, water, and gaseous components different from carbon dioxide or water typically constitute 100 mol of the second gas stream in the split.

[0153] Downstream of the final compression step, a compressed second gas stream is obtained with a pressure of 25 barg to 50 barg, preferably 30 barg to 45 barg.

[0154] Typically, the temperature of the second gas stream increases during each compression step due to the energy introduced during the compression step.

[0155] The temperature of the compressed second gas stream is preferably 75°C to 150°C, more preferably 85°C to 140°C, and even more preferably 90°C to 125°C.

[0156] The compressed second gas stream is cooled to obtain a cooled compressed second gas stream having a pressure of 25 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C.

[0157] The cooling step may be performed in a single cooling step downstream of one or more compression steps.

[0158] Alternatively, downstream of the hydrogenation step and each compression step, the second gas stream is cooled to a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C to obtain a cooled compressed second gas stream.

[0159] Preferably, the cooled compressed gas stream and the cooled compressed second gas stream are combined in a water adsorption unit as described above or below to obtain a combined dry gas stream.

[0160] In the described embodiment, an additional gas stream containing carbon dioxide and water may also be passed through an upstream process stream that generates a cooled compressed gas stream or a cooled compressed second gas stream. All these additional cooled compressed gas streams may be combined with the cooled compressed gas stream and the cooled compressed second gas stream in a water adsorption unit as described above or below to obtain a combined dry gas stream.

[0161] Preferably, at the production site of the method from which these gas flows originate, such as the production site of a method for producing ethylene oxide and / or ethylene glycol and a method for producing ammonia, the gas flow and the second gas flow, as well as any optional additional gas flow, are compressed and cooled to produce a cooled compressed gas flow or a cooled compressed second gas flow.

[0162] Then one or more or all of the cooling compressed gas stream or the cooling compressed second gas stream are delivered to the location of the water adsorption unit in order to adsorb water from the combined cooling compressed gas stream.

[0163] The dry combined gas stream obtained from the water adsorption unit has a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 25 ppm-mol, preferably 0 ppm-mol to 20 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

[0164] In the second embodiment, the total mass flow rate of the drying gas stream is preferably in the range of 48,000 kg / h to 175,000 kg / h, preferably 58,000 kg / h to 165,000 kg / h, and more preferably 65,000 kg / h to 155,000 kg / h.

[0165] Dry gas streams can be used as feed streams in industrial chemical processes or beverage production, or stored in carbon traps.

[0166] Device

[0167] In a second aspect, the present invention relates to an apparatus for purifying a stream of carbon dioxide, the apparatus comprising:

[0168] • A component for reducing the amount of oxygen and / or ethylene in a gas stream, preferably a component for hydrogenating oxygen and / or ethylene, more preferably a hydrogenator, wherein the component for reducing the amount of oxygen and / or ethylene in a gas stream comprises a metal catalyst, preferably a catalyst comprising platinum, palladium and / or ruthenium, more preferably a catalyst comprising platinum or palladium, and preferably supported by a support material.

[0169] • One or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components connected in series for compressing a gas stream, preferably a compressor, wherein the gas stream comprises 30.0 mol% to 99.8 mol% carbon dioxide, 0.1 mol% to 60.0 mol% water, and additionally comprises 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene, or both;

[0170] • In one or more components for compressing a gas stream, preferably downstream of a compressor, components for cooling the compressed gas stream;

[0171] • A water adsorption unit downstream of a component used for cooling a compressed gas stream, for adsorbing water from the cooled compressed gas stream; and

[0172] • A component used to transport a stream of cooled compressed gas from a component used to cool the compressed gas stream to a water adsorption unit.

[0173] The apparatus in the second aspect of the invention as described above or below is preferably adapted to the method of the first aspect of the invention as described above or below.

[0174] One or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components for compressing the gas flow are preferably compressors.

[0175] One or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components for compressing a gas stream are connected in series, preferably via a component for conveying the gas stream from an upstream component for compressing the gas stream to a next downstream component for compressing the gas stream, preferably via a feed line.

[0176] Within a series of one or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components for compressing the gas flow, one or more components for cooling the gas flow may be provided.

[0177] In one embodiment, downstream of each component used to compress the gas flow, a component for cooling the gas flow is provided.

[0178] Preferably, each component for cooling the gas flow is connected to the upstream component for compressing the gas flow via a component for conveying the gas flow from the component for compressing the gas flow to the component for cooling the gas flow (preferably a feed line).

[0179] Furthermore, preferably each of the components for cooling the gas flow is connected to the downstream component for compressing the gas flow via a component for conveying the gas flow from the component for cooling the gas flow to the component for compressing the gas flow (preferably a feed line).

[0180] One or more components used to cool the gas flow are preferably heat exchangers. Preferably, the one or more components used to cool the gas flow are connected to a cooling medium supply source via cooling lines. The cooling medium supply source is preferably a cooling water supply source.

[0181] Preferably, the first upstream component for compressing the gas stream is connected to an upstream chemical industry process via a component (preferably a feed line) of a series of components for compressing the gas stream to deliver the gas stream to one or more components for compressing the gas stream. The gas stream comprises 30.0 mol% to 99.8 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water, and also comprises one or both of 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene.

[0182] The upstream chemical industry process may be a method for producing ethylene oxide and / or ethylene glycol.

[0183] Preferably, the first upstream component for compressing the gas stream is connected to only one upstream chemical industry process.

[0184] The component for reducing the amount of oxygen and / or ethylene in the gas stream is preferably located downstream of one of a series of components for compressing the gas stream, preferably downstream of the second to eighth, preferably the third or fourth, components for compressing the gas stream in a series of one or more components for compressing the gas stream.

[0185] Preferably, the component for reducing the amount of oxygen and / or ethylene in the gas stream is located downstream of one of a series of components for compressing the gas stream, wherein the gas stream reaches a pressure of 3 barg to 12 barg, more preferably 5 barg to 10 barg, and even more preferably 6 barg to 8 barg.

[0186] Preferably, the component for reducing the amount of oxygen and / or ethylene in the gas stream is connected to the component for compressing the gas stream via a component for conveying the gas stream from the component for compressing the gas stream to the component for reducing the amount of oxygen and / or ethylene in the gas stream (preferably a feed line).

[0187] The component for conveying the gas stream from the component for compressing the gas stream to the component for reducing the amount of oxygen and / or ethylene in the gas stream is preferably diverted from the component for conveying the gas stream from an upstream component for compressing the gas stream to a next downstream component for compressing the gas stream.

[0188] Downstream of the component for reducing the amount of oxygen and / or ethylene in the gas stream and upstream of the component for compressing the gas stream, a component for heating the gas stream may be provided.

[0189] The component used to heat the gas flow is preferably a heat exchanger.

[0190] Preferably, the component for heating the gas flow is connected to the component for compressing the gas flow via a component for conveying the gas flow from the component for compressing the gas flow to the component for heating the gas flow (preferably a feed line).

[0191] Preferably, the component for heating the gas flow is connected to the component for reducing the amount of oxygen and / or ethylene in the gas flow by means of a component for conveying the gas flow from the component for heating the gas flow to a component for reducing the amount of oxygen and / or ethylene in the gas flow.

[0192] Preferably, the component for heating the gas flow is connected to a heating source via a heating pipeline. The heating source is preferably a steam source.

[0193] Preferably, upstream of the component for reducing the amount of oxygen and / or ethylene in the gas stream, and preferably upstream of the component for heating the gas stream, the component for conveying the gas stream from the component for compressing the gas stream to the component for reducing the amount of oxygen and / or ethylene in the gas stream is connected to the component for conveying hydrogen from a hydrogen source to the component for reducing the amount of oxygen and / or ethylene in the gas stream.

[0194] Therefore, it is preferable to introduce the combined flow of gas and hydrogen into a component for reducing the amount of oxygen and / or ethylene in the gas flow, and more preferably into a component for heating the gas flow.

[0195] Preferably, the component for reducing the amount of oxygen and / or ethylene in the gas stream is connected to one of a series of components for compressing the gas stream via a component for conveying the gas stream from a component for reducing the amount of oxygen and / or ethylene in the gas stream to a component for compressing the gas stream (preferably a feed line).

[0196] Preferably, downstream of the component for conveying the gas flow from the component for compressing the gas flow to the component for reducing the amount of oxygen and / or ethylene in the gas flow, the component for conveying the gas flow from the component for reducing the amount of oxygen and / or ethylene in the gas flow to the component for compressing the gas flow is connected to the same component for conveying the gas flow from an upstream component for compressing the gas flow to a next downstream component for compressing the gas flow.

[0197] The component for reducing the amount of oxygen and / or ethylene in the gas stream is preferably a component for hydrogenating oxygen and / or ethylene, and more preferably a hydrogenator.

[0198] The component used to reduce the amount of oxygen and / or ethylene in the gas stream is preferably a reactor filled with a metal catalyst bed.

[0199] The metal catalyst is preferably a catalyst containing platinum, palladium and / or ruthenium, more preferably platinum or palladium.

[0200] Metal catalysts are preferably suitable for converting oxygen to water in the presence of hydrogen, and for converting ethylene to ethane in the presence of hydrogen.

[0201] Metal catalysts are preferably supported by a carrier material.

[0202] The carrier material is preferably alumina (Al2O3) or silicon dioxide (SiO2), and preferably sintered alumina.

[0203] Suitable carrier materials include, for example, tablet carriers, extrusions, spheres, and coated monolithic catalysts.

[0204] The tablet carrier preferably has a size of 1 mm × 1 mm to 5 mm × 5 mm, more preferably 2 mm × 2 mm to 4 mm × 4 mm (such as about 3 mm × 3 mm).

[0205] The spherical carrier preferably has an average particle size of 1 mm to 10 mm, more preferably 2 mm to 8 mm (such as 2 mm to 4 mm or about 8 mm).

[0206] Carrier materials are commercially available. Suitable carrier materials are, for example, those named CSS and SAS, such as CSS 350 or SAS 90, which are commercially available from BASF SE.

[0207] Based on the total weight of the metal catalyst and the support material, the metal catalyst is preferably present on the support material in an amount of 0.01% to 1.0% by weight, more preferably 0.02% to 0.7% by weight, and even more preferably 0.05% to 0.5% by weight.

[0208] Metal catalysts can be introduced onto the support material through impregnation.

[0209] Metal catalysts are commercially available. A suitable metal catalyst is, for example, PuriStar, which is commercially available from BASF SE. ® R0-20 or more specifically R0-20 / 25.

[0210] The device also includes a component for cooling the compressed gas stream, located downstream of one or more components for compressing the gas stream, and preferably downstream of components for reducing the amount of oxygen and / or ethylene in the gas stream.

[0211] The component used to cool the compressed gas stream is preferably a heat exchanger.

[0212] Preferably, the component for cooling the compressed gas stream is connected to the final downstream component for compressing the gas stream via a component (preferably a feed line) for conveying the compressed gas stream from the final downstream component for compressing the gas stream to the component for cooling the compressed gas stream.

[0213] Preferably, the components used to cool the compressed gas flow are connected to a cooling medium supply source via cooling lines. The cooling medium supply source is preferably a cooling water supply source.

[0214] The apparatus according to the invention further includes a water adsorption unit downstream of the component for cooling the compressed gas stream for adsorbing water from the cooled compressed gas stream.

[0215] The water adsorption unit is preferably located downstream of the component used to cool the compressed gas stream.

[0216] Preferably, the water adsorption unit is connected to the component for cooling the compressed gas stream via a component for conveying the cooled compressed gas stream from the component for cooling the compressed gas stream to the water adsorption unit.

[0217] The component for conveying a cooling compressed gas stream from the component for cooling the compressed gas stream to the water adsorption unit preferably includes at least one valve for opening or closing the component for conveying the cooling compressed gas stream from the component for cooling the compressed gas stream to the water adsorption unit.

[0218] The water adsorption unit includes at least one container holding the adsorbent.

[0219] The adsorbent is preferably an aluminosilicate.

[0220] Based on the total weight of the aluminosilicate, the aluminosilicate preferably has an alumina (Al2O3) content of 1.0 wt% to 7.5 wt%, more preferably 2.0 wt% to 6.0 wt%, and even more preferably 2.5 wt% to 5.0 wt%.

[0221] Furthermore, based on the total weight of the aluminosilicate, the aluminosilicate preferably has a silicon dioxide (SiO2) content of 92.5% to 99.0% by weight, more preferably 94.0% to 98.0% by weight, and even more preferably 95.0% to 97.5% by weight.

[0222] Preferably, the aluminosilicate is composed of aluminum oxide and silicon dioxide.

[0223] Aluminosilicates are preferably present in the water adsorption unit in the form of gel, and more preferably in the form of gel beads.

[0224] Aluminosilicates preferably have a surface area of ​​500 m² / g to 850 m² / g, more preferably 550 m² / g to 800 m² / g, and even more preferably 600 m² / g to 775 m² / g.

[0225] Furthermore, the aluminosilicate preferably has a pore volume of 0.30 ml / g to 0.55 ml / g, more preferably 0.35 ml / g to 0.50 ml / g, and even more preferably 0.40 ml / g to 0.46 ml / g.

[0226] Furthermore, the pressure dew point of the gas flow around the aluminosilicate is preferably in the range of -50°C to -75°C, more preferably -55°C to -70°C, and even more preferably -57°C to -67°C.

[0227] Furthermore, the desorption temperature of aluminosilicate is preferably in the range of 100°C to 175°C, more preferably 110°C to 165°C, and even more preferably 115°C to 155°C.

[0228] Aluminosilicates are commercially available. Suitable aluminosilicates can be found under the trade name Sorbead. ® (Preferably Sorbead) ®The Air was purchased from BASF SE.

[0229] The water adsorption unit preferably includes at least two sub-units arranged in parallel, more preferably two to five sub-units, and even more preferably three sub-units.

[0230] Each subunit of the water adsorption unit is connected via distribution lines to a component for conveying the compressed gas stream from the final downstream component for compressing the gas stream to a component for cooling the compressed gas stream.

[0231] Each distribution line preferably includes a valve for independently opening or closing the distribution line.

[0232] Preferably, the water adsorption unit is connected to a downstream storage unit for storing a dry gas stream for further use. The dry gas stream has a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 100 ppm-mol, preferably 0 ppm-mol to 50 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

[0233] Preferably, the water adsorption unit is connected to the downstream storage unit via a component (preferably a feed line) for conveying the dry gas stream from the water adsorption unit to the downstream storage unit.

[0234] The component for conveying the dry gas stream from the water adsorption unit to the downstream storage unit preferably includes at least one valve for opening or closing the component for conveying the dry gas stream from the water adsorption unit to the downstream storage unit.

[0235] Preferably, each subunit of the water adsorption unit is connected to a second distribution line. More preferably, the distribution lines of each subunit are joined to form a component for conveying a stream of dry gas from the water adsorption unit to a downstream storage tank.

[0236] Each second distribution line preferably includes a valve for independently opening or closing the second distribution line. The valve is preferably located upstream of the junction of the second distribution line and the component for delivering the dry gas flow to the downstream storage tank.

[0237] The device preferably also includes a route that branches off from the delivery route of the compressed gas stream from the final downstream component for compressing the gas stream, via a component for cooling the compressed gas stream and a water adsorption unit (preferably a sub-unit of the water adsorption unit) to the downstream storage.

[0238] In the diversion route, preferably, the compressed gas stream is conveyed from a component for conveying the compressed gas stream from a final downstream component for compressing the gas stream to a component for cooling the compressed gas stream, via a component for heating the compressed gas stream, to a water adsorption unit, preferably a subunit of the water adsorption unit.

[0239] Preferably, the compressed gas stream is transported from the water adsorption unit (preferably a sub-unit of the water adsorption unit) via a component for cooling the wet compressed gas stream and a component for separating water from the cooled wet compressed gas stream, back to a component for transporting the compressed gas stream from the final downstream component for compressing the gas stream to the component for cooling the compressed gas stream.

[0240] The diversion route is applicable to the adsorbent in the water regeneration adsorption unit, preferably regenerating the adsorbent in each sub-unit of the water adsorption unit independently. Thus, the compressed gas stream heated in the component for heating the compressed gas stream is used to desorb water from the water adsorption unit, preferably from each sub-unit of the water adsorption unit. The desorbed water is then separated from the wet compressed gas stream, which is subsequently recycled back to the water adsorption unit.

[0241] In the diversion route, preferably, the compressed gas flow is delivered via a first diversion line from a component for delivering the compressed gas flow from the final downstream component for compressing the gas flow to a component for cooling the compressed gas flow, and then to a component for heating the compressed gas flow.

[0242] The component used for heating the compressed gas flow is preferably a component used for reducing the pressure of the compressed gas flow, and more preferably an expansion valve.

[0243] By expanding the compressed gas flow, the pressure of the compressed gas flow is reduced, while the temperature is increased through temperature-variable adsorption.

[0244] Preferably, the heated compressed gas stream is delivered from the component for heating the compressed gas stream to the water adsorption unit via a second diversion line. The second diversion line preferably includes at least one valve for opening and closing the second diversion line.

[0245] Preferably, the second branch line is divided into second sub-branch lines, each of which is connected to a sub-unit of the water adsorption unit. Preferably, each second sub-branch line includes a valve for independently opening and closing the second sub-branch line.

[0246] Preferably, the water adsorption unit is connected to a component for cooling the wet compressed gas stream via a third diversion line. The third diversion line preferably includes at least one valve for opening and closing the third diversion line.

[0247] Preferably, each subunit of the water adsorption unit is connected to a third sub-diversion line, which is preferably connected upstream of a valve for opening or closing a component for delivering a dry gas flow from a subunit.

[0248] Preferably, each third sub-shunt line includes a valve for independently opening and closing the third sub-shunt line.

[0249] Preferably, the component for cooling the wet compressed gas stream is connected to the component for separating water from the cooled wet compressed gas stream via a fourth branch line.

[0250] The component used to cool the wet compressed gas stream is preferably a heat exchanger. Preferably, the component for cooling the wet compressed gas stream is connected to a cooling medium supply source via a cooling pipeline. The cooling medium supply source is preferably a cooling water supply source.

[0251] The component used to separate water from the cooled wet compressed gas stream is preferably a water separator known in the art.

[0252] Preferably, the component for separating the water from the cooled wet compressed gas stream is connected via a fifth branch line to the component for conveying the compressed gas stream from the final downstream component for compressing the gas stream to the component for cooling the compressed gas stream.

[0253] Preferably, the fifth branch line is connected downstream of the first branch line to a component for conveying the compressed gas stream from the final downstream component for compressing the gas stream to a component for cooling the compressed gas stream.

[0254] The water adsorption unit can operate in working mode to adsorb water from the cooled compressed gas stream, or in regeneration mode to desorb water from the adsorbent.

[0255] The operating mode or regeneration mode can be activated by adjusting the valves upstream and downstream of the water adsorption unit accordingly.

[0256] To operate the water adsorption unit in working mode, open the valves in the components that supply the cooling compressed gas stream from the cooling component to the water adsorption unit and the valves in the components that supply the dry gas stream from the water adsorption unit to the downstream storage tank. Simultaneously, close the valves in the second and third branch lines.

[0257] To operate the water adsorption unit in regeneration mode, close the valves in the components that supply the cooling compressed gas stream from the cooling components to the water adsorption unit and the valves in the components that supply the dry gas stream from the water adsorption unit to the downstream storage tank. Simultaneously, open the valves in the second and third branch lines.

[0258] In an embodiment where the water adsorption unit includes at least two sub-units arranged in parallel, more preferably two to five sub-units, and even more preferably three sub-units, each sub-unit can be independently switched between working mode and regeneration mode.

[0259] To operate the subunit in working mode, open the valves in the distribution line and the second distribution line connected to the subunit. Simultaneously, close the valves in the second sub-shunt line and the third sub-shunt line connected to the subunit.

[0260] To operate the subunit in regeneration mode, close the valves in the distribution line and the second distribution line connected to the subunit. Simultaneously, open the valves in the second sub-shunt line and the third sub-shunt line connected to the subunit.

[0261] In a preferred embodiment, the water adsorption unit comprises three sub-units arranged in parallel, preferably consisting of three sub-units arranged in parallel.

[0262] In the embodiment described, two of these sub-units preferably operate in working mode, and one sub-unit operates simultaneously in regeneration mode.

[0263] In one embodiment, the apparatus may include more than one set of devices as described above or below. The more than one set of devices includes more than one set of components for compressing the gas stream, more than one component downstream of one or more components for cooling the compressed gas stream, and optionally more than one component for reducing the amount of oxygen and / or ethylene in the gas stream (if present).

[0264] In the more than one set of devices, gas streams from different industrial methods are independently compressed, cooled, and optionally purified from oxygen and / or ethylene when needed.

[0265] Then, upstream of a single water adsorption unit, the cooled compressed gas streams obtained from each component used to cool the compressed gas stream are combined.

[0266] In the embodiment described above, the device further includes:

[0267] A second group of one or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components connected in series for compressing a gas stream, preferably a compressor, the gas stream comprising 90.0 mol% to 99.9 mol% carbon dioxide and 0.1 mol% to 10.0 mol% water;

[0268] In a second group of one or more components for compressing the gas stream, preferably a second component downstream of the compressor for cooling the compressed gas stream;

[0269] A component used to transport a compressed gas stream from a second component used to cool the compressed gas stream to a water adsorption unit.

[0270] Therefore, the second component for compressing the gas stream, the second component for cooling the compressed gas stream, and the component for conveying the compressed gas stream from the second component for cooling the compressed gas stream to the water adsorption unit are preferably arranged and designed in the same manner as the components for compressing the gas stream, cooling the compressed gas stream, and conveying the compressed gas stream from the second component for cooling the compressed gas stream to the water adsorption unit as described above.

[0271] Preferably, upstream of the water adsorption unit, a component for conveying a compressed gas stream from a second component for cooling the compressed gas stream to the water adsorption unit is combined with a component for conveying a compressed gas stream from a component for cooling the compressed gas stream to the water adsorption unit as described above, to form a combined component for conveying a combined compressed gas stream to the water adsorption unit.

[0272] The assembly components used to deliver the combined compressed gas stream to the water adsorption unit are preferably directly connected to the water adsorption unit.

[0273] The more than one set of devices may include more than one component for reducing the amount of oxygen and / or ethylene in the gas stream. Whether there is more than one component for reducing the amount of oxygen and / or ethylene in the more than one set of devices in the more than one set of devices depends on the industrial chemical process downstream of the more than one set of devices.

[0274] Preferably, each set of devices is connected downstream of an industrial chemical process.

[0275] This component for reducing the amount of oxygen and / or ethylene in the gas stream is only needed in the device when there are large amounts of oxygen and / or ethylene in the gas stream.

[0276] When the apparatus is installed downstream of a method for producing ethylene oxide, i.e., when a first upstream component for compressing a gas stream in a series of one or more components for compressing a gas stream is connected to a method for producing ethylene oxide and / or ethylene glycol, a component for reducing the amount of oxygen and / or ethylene in the gas stream is preferably present in the apparatus.

[0277] When the device is installed downstream of a method for producing ammonia, i.e., when a first upstream component for compressing a gas stream in a series of one or more components for compressing a gas stream is connected to a method for producing ammonia, components for reducing the amount of oxygen and / or ethylene in the gas stream are preferably not present in the device.

[0278] use

[0279] In a third aspect, the present invention relates to the use of the methods and / or apparatus described above or below for purifying a carbon dioxide stream derived from an industrial chemical process, preferably from a process for producing ethylene oxide, and for using the purified carbon dioxide stream as a feed stream in a further industrial chemical process or in beverage production or carbon capture and storage.

[0280] Preferably, the use of the third aspect of the invention is applicable to all aspects described with respect to the methods and / or apparatus of the invention as described above or below.

[0281] Detailed description of the attached figures

[0282] pass Figures 1 to 3 Further examples of the invention are provided.

[0283] Figure 1

[0284] Figure 1 A schematic overview of the method and apparatus of the present invention for purifying a carbon dioxide-containing stream originating from a method for producing ethylene oxide is shown.

[0285] First, a gas stream from an ethylene oxide production facility undergoes a first set of compression steps in one or more compressors arranged in series, preferably two to four, more preferably three or four, and even more preferably three. The gas stream has a mass flow rate of 5,000 kg / h to 45,000 kg / h, a CO2 content in the range of about 75.0 mol% to 98.0 mol%, a water content in the range of about 1.0 mol% to 20.0 mol%, an oxygen content of up to 5000 mol-ppm, an ethylene content of up to 1500 mol-ppm, and a pressure of about 5 barg. Downstream of the first set of compression steps, the gas stream, having a pressure of about 6 barg to 8 barg, undergoes a hydrogenation step in a hydrogenator (or deoxygenation reactor) in the presence of hydrogen and a metal catalyst (preferably a supported palladium catalyst). In the hydrogenator, oxygen is converted to water, and ethylene is converted to ethane. Therefore, the gas stream downstream of the hydrogenator has an oxygen content of 0 mol-ppm to 50 mol-ppm and an ethylene content of 0 mol-ppm to 7.5 mol-ppm. The gas stream downstream of the hydrogenator undergoes a second set of compression steps in one or more, preferably two to four, more preferably three or four, and even more preferably three compressors arranged in series to reach a pressure of 30 barg to 45 barg. The compressed gas stream is cooled in a heat exchanger and undergoes a water adsorption step in a water adsorption unit (or drying unit) containing aluminosilicate as an adsorbent. A dry compressed gas stream with a CO2 content in the range of about 97.5 mol% to 100 mol%, a water content of 0 mol% to 0.05 mol%, an oxygen content of 0 mol-ppm to 50 mol-ppm, an ethylene content of 0 mol-ppm to 7.5 mol-ppm, and a pressure of 30 barg to 45 barg is delivered from the water adsorption unit to the CO2 network for further use. The dry compressed gas stream has a mass flow rate of 4,500 kg / h to 45,000 kg / h.

[0286] Figure 1 Each method step illustrated is indicated by numbers 1 to 7.

[0287] Figure 2 :

[0288] Figure 2 A schematic overview of the method and apparatus of the present invention for purifying carbon dioxide-containing streams derived from methods for producing ethylene oxide and from methods for producing ammonia, the streams being combined in a water adsorption unit, is shown.

[0289] Therefore, in Figure 2 The lower part, for the method used to produce ethylene oxide, adopts the same approach as... Figure 1 The methods and apparatus used are the same.

[0290] exist Figure 2 The upper part shows a schematic overview of the method and apparatus of the present invention for purifying a carbon dioxide-containing stream originating from a method for producing ammonia.

[0291] Thus, the gas stream from the ammonia production facility is first subjected to a first set of compression steps in one or more, preferably one or two, more preferably one compressor (more than one compressor arranged in series), to reach a pressure of 0.5 barg to 1.0 barg. The gas stream has a mass flow rate of 70,000 kg / h to 125,000 kg / h, a CO2 content of 80.0 mol% to 99.0 mol%, a water content of 1.0 mol% to 20.0 mol%, and a pressure of approximately 40 mbarg. Downstream of the first set of compression steps, a portion of the gas stream can be diverted from this method and delivered to a carbon capture unit (CCU). The downstream gas stream now has a mass flow rate of 70,000 kg / h to 100,000 kg / h and undergoes a second set of compression steps in one or more, preferably two to six, more preferably three or four, and even more preferably four compressors arranged in series, to reach a pressure of 350 barg to 45 barg. The compressed gas stream is cooled in a heat exchanger and undergoes a water adsorption step in a water adsorption unit (or drying unit) containing aluminosilicate as an adsorbent. In the water adsorption unit, the compressed gas stream is combined with a combined compressed gas stream from a dried combined compressed gas stream having a CO2 content in the range of approximately 97.5 mol% to 100 mol%, a water content in the range of 0 mol% to 0.05 mol%, an oxygen content in the range of 0 mol-ppm to 20 mol-ppm, and an ethylene content in the range of 0 mol-ppm to 7.5 mol-ppm. The compressed gas stream is then conveyed from the water adsorption unit to a CO2 network for further use. The combined dried combined compressed gas stream has a mass flow rate of 65,000 kg / h to 155,000 kg / h.

[0292] Figure 2 Each method step illustrated is indicated by numbers 1 to 12.

[0293] Figure 3 :

[0294] Figure 3 A schematic overview of a preferred embodiment of a water adsorption unit with three sub-units arranged in parallel is shown, wherein two sub-units (beds A and B) operate in working mode and one sub-unit (bed C) operates in regeneration mode.

[0295] For beds A and B, a cooled and compressed gas stream with a pressure of approximately 35 barg and a temperature of approximately 40°C is introduced downstream of a heat exchanger (not shown). This is indicated by a white valve symbol upstream of beds A and B, indicating an open valve. Water is adsorbed from the cooled and compressed gas stream in beds A and B. The dried gas stream obtained from beds A and B is then delivered to the CO2 network for further use via the open valve (white valve symbol). The regeneration gas circulation for beds A and B is shut off as indicated by the black valve symbol.

[0296] For bed C, the compressed gas stream is split and heated in a regenerated gas heater. As indicated by the white valve symbol, a heated compressed gas stream with a pressure of approximately 35 barg and a temperature of approximately 160°C is introduced into bed C. The temperature of the heated compressed stream falls within the desorption temperature range of the aluminosilicate adsorbent (120°C to 150°C), causing water to desorb from bed C. The wet, heated compressed gas stream is cooled in a regenerated gas cooler and dried in a regenerated gas separator (indicated by the white valve symbol). The dried regenerated gas is then recirculated back into the compressed gas stream.

[0297] As indicated by the black valve symbol, the water adsorption delivery has been shut off.

[0298] In an exemplary method, beds A and B operate in operating mode (adsorption mode) for two-thirds of the time increment (e.g., 40 minutes), while bed C operates in regeneration mode for one-third of the time increment (e.g., 20 minutes). After the stated one-third time increment (e.g., 20 minutes), bed C is switched back to operating mode by adjusting the corresponding valve, while bed A is switched back to regeneration mode. After another one-third time increment (e.g., 20 minutes), bed A is switched back to operating mode by adjusting the corresponding valve, while bed B is switched back to regeneration mode. After yet another one-third time increment (e.g., 20 minutes), bed B is switched back to operating mode by adjusting the corresponding valve, while bed C is switched back to regeneration mode.

Claims

1. A method for purifying a carbon dioxide stream, the method comprising the following steps: • Provide a gas stream comprising 30.0 mol% to 99.8 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water, and additionally comprising one or both of 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene; • In the presence of a metal catalyst, the gas stream is subjected to a hydrogenation step for removing oxygen and / or ethylene from the gas stream, wherein the metal catalyst is preferably a catalyst containing platinum, palladium and / or ruthenium, more preferably a catalyst containing platinum or palladium, and preferably supported by a support material. • The gas stream is subjected to one or more compression steps to obtain a compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg; • The compressed gas stream is cooled downstream of the hydrogenation step and the one or more compression steps to obtain a cooled compressed gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C. • Water is adsorbed from the cooled compressed gas stream in the water adsorption unit to obtain a dry gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 100 ppm-mol, preferably 0 ppm-mol to 50 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

2. The method according to claim 1, wherein the gas stream originates from a method for producing ethylene oxide and / or ethylene glycol.

3. The method according to any one of the preceding claims, wherein the gas stream is compressed to a pressure of 3 barg to 12 barg, preferably 5 barg to 10 barg, more preferably 6 barg to 8 barg before hydrogenation.

4. The method according to any one of the preceding claims, wherein in the hydrogenation step, the gas stream is subjected to a stream containing 99.0 mol% to 100 mol% hydrogen, the stream preferably having a pressure of 3 barg to 12 barg, more preferably 5 barg to 10 barg, even more preferably 6 barg to 9 barg and / or preferably a temperature of 10°C to 45°C, more preferably 12°C to 40°C, and more preferably a pressure 0.1 barg to 1.0 barg, preferably 0.2 barg to 0.5 barg higher than the compressed gas stream before hydrogenation.

5. The method according to any one of the preceding claims, wherein the gas stream is subjected to two to ten compression steps, preferably three to eight compression steps, and more preferably five to six compression steps to obtain the compressed gas stream.

6. The method according to any one of the preceding claims, wherein the water adsorption unit comprises aluminosilicate as an adsorbent.

7. The method according to any one of the preceding claims, wherein during the regeneration mode, adsorbed water is removed from the adsorbent by temperature-switching adsorption.

8. The method according to any one of the preceding claims, wherein the total mass flow rate of the gas stream is in the range of 2,500 kg / h to 60,000 kg / h, preferably 3,000 kg / h to 50,000 kg / h, more preferably 5,000 kg / h to 45,000 kg / h.

9. The method according to any one of the preceding claims, further comprising the following steps: • Provide a second gas stream comprising 40.0 mol% to 99.9 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water; • The second gas stream is subjected to one or more compression steps to obtain a compressed second gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg; • The compressed second gas stream is cooled downstream of the hydrogenation step and the one or more compression steps to obtain a cooled compressed second gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, preferably 30 barg to 45 barg and a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C. • The cooled compressed second gas flow and the cooled compressed gas flow are combined to obtain a combined compressed gas flow; as well as • Water is adsorbed from the combined cooled compressed gas stream in the water adsorption unit to obtain a dry combined gas stream having a pressure of 20 barg to 50 barg, preferably 25 barg to 47 barg, more preferably 30 barg to 45 barg, a temperature of 25°C to 55°C, preferably 30°C to 50°C, more preferably 35°C to 45°C, an oxygen content of less than 25 ppm-mol, preferably 0 ppm-mol to 20 ppm-mol, an ethylene content of less than 10 ppm-mol, preferably 0 ppm-mol to 7.5 ppm-mol, a water content of less than 0.1 mol%, preferably 0 mol% to 0.05 mol%, more preferably 0 mol% to 0.02 mol%, and a carbon dioxide content of 96.5 mol% to 100 mol%, preferably 97.0 mol% to 100 mol%, more preferably 97.5 mol% to 100 mol%.

10. The method of claim 9, wherein the second gas stream originates from a method for producing ammonia.

11. The method according to any one of the preceding claims, wherein the dry gas stream is used as a feed stream in an industrial chemical process or in beverage production or stored in a carbon trap.

12. An apparatus for purifying a carbon dioxide stream, the apparatus comprising: • A component for reducing the amount of oxygen and / or ethylene in the gas stream, preferably a component for hydrogenating oxygen and / or ethylene, more preferably a hydrogenator, wherein the component for reducing the amount of oxygen and / or ethylene in the gas stream comprises a metal catalyst, preferably a catalyst containing platinum, palladium and / or ruthenium, more preferably a catalyst containing platinum or palladium, and preferably supported by a support material. • One or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components connected in series for compressing a gas stream, preferably a compressor, the gas stream comprising 30.0 mol% to 99.8 mol% carbon dioxide, 0.1 mol% to 60.0 mol% water, and additionally comprising 25 mol-ppm to 10000 mol-ppm, preferably 50 mol-ppm to 7500 mol-ppm, more preferably 100 mol-ppm to 5000 mol-ppm oxygen and / or 10 mol-ppm to 5000 mol-ppm, preferably 25 mol-ppm to 2500 mol-ppm, more preferably 50 mol-ppm to 1500 mol-ppm ethylene, or both; • A component for cooling the compressed gas flow, preferably downstream of a compressor, in one or more components for compressing the gas flow; • A water adsorption unit downstream of the component used to cool the compressed gas stream for adsorbing water from the cooled compressed gas stream; as well as • A component for conveying the cooled compressed gas stream from the component for cooling the compressed gas stream to the water adsorption unit.

13. The apparatus according to claim 12, wherein the water adsorption unit comprises at least two sub-units arranged in parallel, preferably two to five sub-units, more preferably three sub-units.

14. The apparatus according to any one of claims 12 or 13, further comprising: • A second group of one or more, preferably two to ten, more preferably three to eight, and even more preferably five to six components connected in series for compressing a gas stream, preferably a compressor, the gas stream comprising 40.0 mol% to 99.9 mol% carbon dioxide and 0.1 mol% to 60.0 mol% water; • In the second group of one or more components for compressing the gas stream, preferably a second component downstream of the compressor for cooling the compressed gas stream; • A component for conveying the compressed gas stream from the second component for cooling the compressed gas stream to the water adsorption unit.

15. The method and / or apparatus according to any one of the preceding claims for purifying a carbon dioxide stream derived from an industrial chemical process, preferably from a process for producing ethylene oxide, and for using the purified carbon dioxide stream as a feed stream in a further industrial chemical process or in beverage production or carbon capture and storage.

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