WO2015176713A1 - Procédé et dispositif pour extraire du dioxyde de carbone à partir de mélanges gazeux - Google Patents

Procédé et dispositif pour extraire du dioxyde de carbone à partir de mélanges gazeux Download PDF

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Publication number
WO2015176713A1
WO2015176713A1 PCT/DE2015/100204 DE2015100204W WO2015176713A1 WO 2015176713 A1 WO2015176713 A1 WO 2015176713A1 DE 2015100204 W DE2015100204 W DE 2015100204W WO 2015176713 A1 WO2015176713 A1 WO 2015176713A1
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Prior art keywords
absorbent
carbon dioxide
gas mixture
heater
loaded
Prior art date
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PCT/DE2015/100204
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German (de)
English (en)
Inventor
Onkar DIXIT
Norbert Mollekopf
Original Assignee
Technische Universität Dresden
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Technische Universität Dresden filed Critical Technische Universität Dresden
Publication of WO2015176713A1 publication Critical patent/WO2015176713A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B01D2252/2023—Glycols, diols or their derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20405—Monoamines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20421—Primary amines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/50—Combinations of absorbents
    • B01D2252/502—Combinations of absorbents having two or more functionalities in the same molecule other than alkanolamine
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/60—Additives
    • B01D2252/604—Stabilisers or agents inhibiting degradation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the invention relates to a process for the production of carbon dioxide from gas mixtures. It further relates to an apparatus for carrying out the method.
  • the components to be separated may be impurities that must be removed from the gas mixture before the purified gas mixture can be supplied to its destination. It may vary in the components though also to substances that are to be obtained from the gas mixture in order to be used for a specific purpose.
  • the detergent must be chosen according to the composition of the gas mixture and the nature of the components to be separated from the gas mixture.
  • the process for the purification of gases described in DE 10 2004 042 418 A1 provides for the use of a washing liquid which contains polyalkylene glycol amines.
  • the washing liquid proposed there may contain solvents, for example diglycolamine.
  • the washing liquid should be suitable for separating a plurality of impurities from any gas mixtures, in particular also for the separation of carbon dioxide together with other impurities.
  • DE 10 2004 042 418 AI provides pressures between 1 and 110 bar and temperatures of 0 to 100 ° C before. In the examples, temperatures of 30 ° C and pressures of 50 bar are used to separate carbon dioxide from synthesis gas.
  • the aim of the process described in DE 10 2004 042 418 A1 is the purification of the gas mixture, but not the recovery of carbon dioxide.
  • For the separation of carbon dioxide from biogas, sewage or landfill gas in particular monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA) and water as detergent, which is also referred to as absorbent, are used according to the prior art.
  • Formulations using these absorbents are sold, for example, under the trade name "OASE Green” by BASF SE, Ludwigshafen, Germany
  • the known absorbents may be used in some cases not only at elevated pressure but also at atmospheric pressure.
  • the known methods, which are based on the use of these Abso tion medium require considerable energy input, both in the form of heat energy and in the form of electric current.
  • the object of the invention is to eliminate the disadvantages of the prior art.
  • a method for the recovery of carbon dioxide from a gas mixture is specified, which requires a low energy input.
  • a device suitable for carrying out this method should be
  • the gas mixture contains 20 to 90% by volume of carbon dioxide before being brought into contact with the absorbent.
  • the terms "separation of carbon dioxide from a gas mixture” and “recovery of carbon dioxide from a gas mixture” are used interchangeably.
  • the gas mixture from which carbon dioxide is to be separated according to the invention is also referred to below as the crude gas mixture.
  • the carbon dioxide-containing crude gas mixture is separated into carbon dioxide and a residue which contains no carbon dioxide or up to 4% by volume of carbon dioxide, based on the volume of the remainder.
  • the remainder may be a gas mixture.
  • the remainder may also be referred to as "gas mixture without carbon dioxide", even though it may contain up to 4% by volume of carbon dioxide.
  • the carbon dioxide contained in the crude gas mixture is absorbed by the absorbent
  • Other components of the raw gas mixture will not become absorbed by the absorbent
  • the inventors, without wishing to be bound by theory, are of the opinion that the carbon dioxide is bound by chemical reaction and physical dissolution in the absorbent.
  • the crude gas mixture may be any gas mixture.
  • the crude gas mixture is selected from the group consisting of sewage gas, landfill gas, biogas, synthesis gas, flue gas or natural gas.
  • the gas mixture is a biogas.
  • biogas is understood to mean, in particular, a gas mixture which contains carbon dioxide and methane Hydrogen sulfide included.
  • a typical biogas contains about 35% by volume of carbon dioxide and about 60% by volume of methane (Römpp, Lexikon der Chemie, CD-ROM 1995). Biogases can be produced by the bacterial decomposition of organic matter.
  • the process of the invention makes it possible to separate a crude gas mixture containing carbon dioxide and methane into a first fraction containing carbon dioxide and a second fraction containing methane.
  • the composition of the second fraction may correspond to that of natural gas, in particular H gas.
  • H-gas is understood here as a natural gas containing at least 96 vol .-% methane.
  • H gas corresponds to the definition of H gas in Germany.
  • the method according to the invention thus makes it possible, in particular, to treat biogas at natural gas level at atmospheric pressure, thereby obtaining natural gas (CH 4 ) and carbon dioxide in a sustainable manner, and in addition with reduced energy consumption during gas treatment.
  • the crude gas mixture preferably contains 30 to 90% by volume of carbon dioxide, more preferably 30 to 80% by volume of carbon dioxide, even more preferably 30 to 50% by volume of carbon dioxide and particularly preferably 40% by volume of carbon dioxide.
  • the crude gas mixture may contain methane in addition to carbon dioxide.
  • the crude gas mixture contains carbon dioxide in a proportion of 30 to 50% by volume and methane (CH 4 ) in a proportion of 70 to 30% by volume.
  • the proportion of both components in the crude gas mixture can be between 80 and 100% by volume.
  • the data relate to the volume of the crude gas mixture before the start of the process.
  • the carbon dioxide obtained by means of the process according to the invention has a purity of at least 99% by volume.
  • the figure refers to the volume of carbon dioxide recovered at the end of the process.
  • the absorbent is an aqueous diglycolamine solution.
  • the absorbent according to the invention contains 65 to 85% by weight of diglycolamine.
  • the absorbent contains from 65 to 75% by weight of diglycolamine, more preferably from 70 to 80% by weight of diglycolamine, and most preferably 70% by weight of diglycolamine.
  • the data relate to the mass of Absoiptionsffens before the absorption of carbon dioxide.
  • the molar ratio of diglycolamine in the absorbent on the one hand to carbon dioxide in the gas mixture on the other hand is preferably in the range from 2 to 16, more preferably 4 to 12 and most preferably 2 to 8 at the beginning of the process.
  • the absorbent is preferably used at ambient temperature and pressure , The absorbent is used as a washing liquid for the gas mixture.
  • the carbon dioxide loading in Absoiptionsstoff before the absorbent is brought into contact with the raw gas mixture between 0.04 and 0.20, preferably between 0.06 and 0, 16 moles of carbon dioxide per mole of diglycolamine and water ,
  • mol diglycolamine and water is meant the sum of mol of diglycolamine and mol of water in the absorbing agent.
  • the absorbent may contain 0 to 5 mass% of an oxygen inhibitor.
  • the oxygen inhibitor should be a soluble, especially an absorber-soluble and / or water-soluble oxygen inhibitor.
  • the oxygen inhibitor is a metal salt of etidronic acid, which metal is preferably selected from the group consisting of zinc (Zn), copper (Cu), iron (Fe), and combinations thereof.
  • Huntsman International LLC, USA markets such an oxygen inhibitor under the trade name "Jefftreat AO 832".
  • the crude gas mixture at a temperature of 10 to 40 ° C, preferably at ambient temperature, brought into contact with the absorbent.
  • the crude gas mixture is brought into contact with the absorbent at a pressure of 0.4 to 2 bar, more preferably 1 to 2 bar, even more preferably 1 to 1.8 bar, and most preferably at atmospheric pressure.
  • the pressure data refer to the absolute pressure.
  • the crude gas mixture is saturated with water or at least almost saturated before it comes in contact with the absorbent.
  • the crude gas mixture is considered to be almost saturated with water if it contains at least 90% by volume of the saturation amount of water in the crude gas mixture.
  • the saturation with water is also carried out at a temperature of 10 to 40 ° C, preferably at ambient temperature.
  • the saturation with water is carried out at a pressure of 1 to 2 bar, preferably at atmospheric pressure. More preferably, the saturation of the crude gas mixture with water is carried out at the same pressure and at the same temperature at which the raw gas mixture is brought into contact with the absorbent.
  • the pressure data refer to the absolute pressure.
  • the crude gas mixture may be moistened with water in a humidifier before it comes into contact with the absorbent.
  • the humidifier may be, for example, a bubble column, a Venturi scrubber, a spray scrubber, a jet scrubber, a packed column or a packed column, the list not being exhaustive.
  • the crude gas mixture before it comes into contact with the absorbent, of one or more of the compounds hydrogen sulfide (H 2 S), carbonyl sulfide (COS), methanethiol (CH - SH) and ammonia (NH 3 ), provided it is not already free of these compounds or contains the compounds only in acceptable trace amounts.
  • a trace amount of such a compound of less than 100 ppm, more preferably less than 50 ppm, and even more preferably 5 ppm or less is acceptable. It may be provided that the crude gas mixture before being brought into contact with the absorbent of a treatment for removing at least one of said compounds from the crude gas mixture is subjected.
  • the content of hydrogen sulfide (H 2 S), carbonyl sulfide (COS), methanethiol (CH 3 -SH) and / or ammonia (NH 3 ) in the raw gas mixture may be less than 100 ppm, more preferably less than 50 ppm and even more preferably 5 ppm or less. It is preferred that no oxygen (0 2 ) is needed for the treatment.
  • the raw gas mixture is purified of hydrogen sulfide (H 2 S) before it comes into contact with the absorbent.
  • the crude gas mixture is particularly preferably purified from the sulfur-containing compounds hydrogen sulfide (H 2 S), carbonyl sulfide (COS) and methanethiol (CH 3 -SH). It is preferable that the sum of all the contents of these sulfur-containing compounds is less than 100 ppm, more preferably less than 50 ppm, and even more preferably 5 ppm or less.
  • the purification can be carried out by means of the above-described purification.
  • the crude gas mixture before it comes in contact with the absorbent, 0 to 2 vol .-% oxygen (0 2 ) included.
  • the crude gas mixture is brought into contact with the absorbent by the raw gas mixture is passed as a gas stream through the absorbent.
  • the crude gas mixture is passed in countercurrent to the absorbent.
  • the raw gas mixture can be brought into contact with the absorbent in an absorber.
  • the absorber may be an absorption column.
  • the raw gas mixture and the absorbent are guided in the absorber so that the gas stream rises in countercurrent to the absorbent in the absorber. It will be in the Gas stream contained carbon dioxide absorbed by the absorbent.
  • the loaded with carbon dioxide absorbent expediently at the bottom of the absorber from this.
  • the carbon dioxide-laden absorbent is also referred to below as a loaded absorbent.
  • the remaining part of the gas stream passes as a residual gas stream expediently at the head of the absorber from this. If the crude gas mixture was biogas, then this residual gas stream contains essentially methane. The residual gas stream may already have natural gas quality. Contains the remaining part of the gas stream methane, the residual gas stream can be used as desired for the production of electricity, for the production of heat, for use as fuel or for use as a raw material thereof.
  • the absorber may contain filler or one or more internals.
  • the fillers may be metal fillers, plastic fillers, ceramic fillers, or mixtures of these fillers.
  • the fillers preferably have a specific surface area of 50 to 800 m 2 / m 3 , more preferably 50 to 400 m 2 / m 3 .
  • the fillers are expediently present as a random packed bed in the absorber.
  • the installation may be an installation of a material such as metal, plastic or ceramic or combinations thereof.
  • the installation can also be in the form of structured packings.
  • the incorporation preferably has a specific surface area of 50 to 800 m 2 / m 3 , more preferably 50 to 400 m 2 / m 3 .
  • the absorber is preferably made of metal or glass.
  • the loaded absorbent may be exposed to an elevated temperature, reduced or increased pressure or combination thereof.
  • An elevated temperature is a temperature which is above the temperature at which the crude gas mixture was brought into contact with the absorbent.
  • a reduced pressure is a pressure which is below the pressure at which the crude gas mixture was brought into contact with the absorbent.
  • An elevated one Pressure is a pressure that is above the pressure at which the gas mixture was brought into contact with the absorbent.
  • the loaded absorbent is exposed to an elevated temperature while the pressure is equal to the pressure at which the crude gas mixture has been brought into contact with the absorbent.
  • a separation of the carbon dioxide is provided in two stages. In a first stage, the loaded absorbent is heated to a temperature of 90 to 120 ° C in a first heater. Subsequently, the heated loaded absorbent is transferred by passing a desorber in a second heater. There, the loaded absorbent is heated to a temperature of 100 to 130 ° C.
  • the first heater may be a preheater.
  • the second heater may be a sump heater.
  • step (d) transferring the loaded absorbent obtained in step (c) from the desorber into a second heater; (e) heating the loaded absorbent to a temperature of 100 to 130 ° C in the second heater; (f) transferring the loaded absorbent from the second heater into the desorber;
  • step (c) a loaded absorbent containing less carbon dioxide than the loaded absorbent in step (a) is obtained.
  • step (g) a loaded absorbent containing less carbon dioxide than the loaded absorbent obtained in step (c) is obtained. It can be provided that the Absoiptionsstoff obtained in step (g), as far as technically possible, is free of carbon dioxide.
  • the intended for the separation of carbon dioxide from the loaded absorbent desorber is preferably made of metal or glass. This is expediently a desorption column.
  • the desorber may contain one or more internals in the form of structured packings or packing.
  • the structured packings or packings preferably have a specific surface area of from 50 to 800 m 2 / m 3 , more preferably from 200 to 800 m 2 / m 3, and most preferably from 200 to 400 m 2 / m 3 .
  • the fixtures may be made of a material such as metal, plastic, ceramic or combinations of these materials.
  • the separated from the absorbent carbon dioxide gas stream exits at the head of the desorber, while the purified absorbent at the bottom of the desorber emerges from this
  • Carbon dioxide crude gas Ström can then be passed to a purification device in which Ström in the carbon dioxide raw gas contained residues of ⁇ 08 ⁇ ⁇ 8 ⁇ 6 ⁇ 8, especially vapors of diglycolamine, water or both, are separated from the carbon dioxide.
  • the cleaning device may be a combination of a condenser and an adsorber.
  • the temperature of the carbon dioxide raw gas stream is lowered so that it condenses contained residues of the absorbent.
  • the condensate can be returned to the desorber.
  • the adsorber remaining residues of the absorbent are completely removed.
  • the crude carbon dioxide gas Ström is transferred into a purified gas stream containing at least 99 vol .-% carbon dioxide.
  • the absorbent emerging at the bottom of the desorber is completely or at least partially purified of carbon dioxide and can be recycled back to the absorber.
  • the heating of the loaded absorbent in the first heater and the second heater may be accomplished using electric power or heat.
  • water vapor, a liquid such as fuel oil or combinations thereof may be used.
  • the process according to the invention can be carried out as a continuous process.
  • the process according to the invention makes it possible to recirculate the absorbent.
  • a device for obtaining carbon dioxide having a purity of at least 99% by volume from a gas mixture, which is also referred to as a raw gas mixture, using an Absoiptionsffens for the carbon dioxide is also provided.
  • the apparatus comprises an absorber for contacting the raw gas mixture with the absorbent and a desorber for separating carbon dioxide from the absorbent.
  • the device according to the invention is intended in particular for carrying out the method according to the invention. Details of the device according to the invention have been described above in connection with the method according to the invention. To avoid repetition, reference is made to these details. According to the invention, moreover, the use of an absorbent which
  • Fig. 2 is a detailed view of the embodiment shown in Fig. 1.
  • the embodiment illustrates the recovery of carbon dioxide from a gas mixture, the crude gas mixture.
  • the crude gas mixture is a mixture of carbon dioxide (C0 2 ) and nitrogen (N 2 ).
  • the gas mixture is fed via a line 1 to a humidifier 2.
  • the gas mixture has a volume flow of 2.5 Nm / h.
  • the gas mixture is saturated with water at atmospheric pressure and ambient temperature.
  • Via line 3 the water-saturated gas mixture is fed to an absorption column 4.
  • the absorption column 4 has a nominal diameter of DN 100, which corresponds to an inner diameter of 105.3 mm.
  • the absorption column has a 3 m high area containing metal packing. This area is referred to below as the packed area 5.
  • the packing has a diameter of 15 mm. They are commercially available under the trade name "Novalox-M" (manufacturer: United Art Economics-Fabriken GmbH & Co. KG, Ransbach-Baumbach, Germany).
  • the water-saturated gas mixture enters via line 3 laterally into the absorption column 4 in a region which is above the bottom of the absorption column 4 and below the packing area 5.
  • Via line 6 washing liquid is fed into the absorption column 4.
  • the washing liquid enters via line 6 by means of a ring distributor in the absorption column 4 in an area under the head of the Absorption column 4 and over the packing area 5 is located.
  • the washing liquid flows from top to bottom through the filling body region 5 and comes into contact with the gas mixture which flows through the filling body region 5 from bottom to top. In this case, carbon dioxide contained in the gas mixture is absorbed in the washing liquid.
  • the residual gas stream which consists of remaining components of the gas mixture - in the present embodiment, from 0 to 4 vol .-% C0 2 and the balance nitrogen - occurs at the top of the absorption column 4 from this. It can be continued from the head of the absorption column 4 via line 7.
  • the residual gas stream can be regarded as a "gas mixture without carbon dioxide".
  • the washing liquid is an aqueous solution containing 70% by weight of diglycolamine.
  • the washing liquid is the absorbent provided according to the invention.
  • the scrubbing liquid in which carbon dioxide is absorbed from the gas mixture is referred to below as laden scrubbing liquid.
  • the loaded washing liquid corresponds to the laden Absoiptionsstoff.
  • the detergent circulating rate is 100 kg / h.
  • a line 8 is provided, via which the laden washing liquid is fed using a first feed pump 28 to a heat exchanger 9.
  • line 8 enters the loaded washing liquid at a temperature of 35 ° C.
  • the temperature of the loaded washing liquid increases to 70 ° C.
  • the loaded washing liquid is passed in countercurrent to a stream of purified washing liquid.
  • the loaded washing liquid leaves the heat exchanger 9 at a temperature of 70 ° C via line 10, which leads to a preheater 11. There, the temperature of the loaded scrubbing liquid is raised to 95 ° C.
  • the now 95 ° C hot laden scrubbing liquid is passed via line 12 to a desorption column 13.
  • the desorption column 13 has a nominal diameter of DN 100, which corresponds to an inner diameter of 105.3 mm.
  • the desorption column 13 has two 1.5 m high areas containing structured metal packings. The two areas are referred to below as packing areas 14.
  • the two packing regions 14 are spaced apart from one another, forming a first inlet region 15, into which the 95 ° C hot laden washing liquid enters via the side wall of the desorption column 13 by means of a ring distributor.
  • the structured packings are commercially available under the trade name "Mellapak 250Y” (manufacturer: Sulzer Chemtech Ltd., Winterthur, Switzerland).
  • the loaded scrubbing liquid entering the first inlet region 15 of the desorption column 13 first flows downwards in the desorption column 13 under contact with the structured packing of the lower packing region 14. It cools down slightly. In this case, a first part of the carbon dioxide contained in the loaded washing liquid is released. This first part rises to the top of the desorption column 13.
  • Via line 17, the loaded scrubbing liquid from desorption column 13 is passed to a sump heater 18 (arrow A in FIG.
  • FIG. 2 further illustrates the conditions at the first exit region 16.
  • the desorption column 13 When the device is put into operation, the desorption column 13 is filled with the scrubbing liquid, which is designated by reference numeral 33 in FIG. 2, until it reaches the height of the first exit region 16, starting from the bottom of the desorption column 13. The then entering the desorption column 13 washing liquid 33 flows via line 17 in the sump heater 18 (arrow A) and is heated there to 105 ° C, whereby a second part of carbon dioxide is released, which flows in the desorption column 13 via line 17 (arrow C).
  • the level of the washing liquid 33 in the desorption column 13 can be regulated by means of an automatic or manual control device. In this way it is ensured that washing liquid 33 does not close the first outlet region 16.
  • the upper packing region 14 in the desorption column is intended in particular to bring about condensation of the water or diglycolamine contained in the washing liquid or both.
  • the first and second part of the released carbon dioxide are passed via line 21 as a carbon dioxide crude gas stream to a condenser 22, is separated in the scrubbing liquid contained in the carbon dioxide crude gas stream and recycled via line 30 into the desorption.
  • the carbon dioxide crude gas stream then passes via line 31 to an adsorber 32, in which still remaining scrubbing liquid in the carbon dioxide crude gas stream is separated by means of an adsorbent.
  • the adsorber 32 now exits via line 23, a purified gas stream containing at least 99 vol .-% carbon dioxide.
  • a vacuum pump located downstream of the head of the desorption column 13 to withdraw the carbon dioxide raw gas stream from the desorption column 13. This is not necessary.
  • the purified and thus regenerated washing liquid occurs out.
  • the regenerated scrubbing liquid is passed via line 25 using a second feed pump 29 to the heat exchanger 9, where heat is transferred from the regenerated scrubbing liquid to the laden scrubbing liquid.
  • the thereby cooled regenerated scrubbing liquid is passed via line 26 from the heat exchanger 9 to a cooler 27, in which the regenerated scrubbing liquid is further cooled to a temperature of 12 ° C. From the condenser 27, the 12 ° C cold regenerated scrubbing liquid then passes via line 6 into the absorption column 4.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé pour extraire du dioxyde de carbone présentant une pureté d'au moins 99 % en volume à partir d'un mélange gazeux, ledit mélange gazeux étant mis en contact avec un agent d'absorption pour le dioxyde de carbone. A cet effet, il est prévu que l'agent d'absorption contienne de 65 à 85 % en masse de diglycolamine, de 0 à 5 % en masse d'un inhibiteur d'oxygène et de l'eau pour compléter, et le mélange gazeux contient de 20 à 90 % en volume de dioxyde de carbone avant d'être mis en contact avec l'agent d'absorption. L'invention concerne en outre un dispositif adapté à la réalisation du procédé.
PCT/DE2015/100204 2014-05-21 2015-05-20 Procédé et dispositif pour extraire du dioxyde de carbone à partir de mélanges gazeux WO2015176713A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102014107184.0 2014-05-21
DE102014107184.0A DE102014107184A1 (de) 2014-05-21 2014-05-21 Verfahren und Vorrichtung zur Abtrennung von Kohlendioxid aus Gasgemischen

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WO2015176713A1 true WO2015176713A1 (fr) 2015-11-26

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WO (1) WO2015176713A1 (fr)

Citations (5)

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FR2970423A1 (fr) * 2011-01-19 2012-07-20 IFP Energies Nouvelles Solution absorbante contenant une combinaison d'hinhibiteurs de degradation comportant un derive d'un triazole ou d'un tetrazole et procede d'absorption de composes acides contenus dans un gaz
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FR2994861B1 (fr) * 2012-08-30 2014-08-22 IFP Energies Nouvelles Procede d'absorption de composes acides contenus dans un effluent gazeux au moyen d'une solution aqueuse a base d'amine

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EP1582250A2 (fr) * 2004-03-09 2005-10-05 Basf Aktiengesellschaft Absorbant avec une réstistance améliorée à l'oxidation et procédé pour désacidifier des courants de fluides
DE102004042418A1 (de) 2004-09-02 2006-03-23 Clariant Gmbh Verfahren zur Reinigung von Gasen
WO2008086812A1 (fr) * 2007-01-17 2008-07-24 Union Engineering A/S Procédé de récupération de dioxyde de carbone à pureté élevée
FR2970423A1 (fr) * 2011-01-19 2012-07-20 IFP Energies Nouvelles Solution absorbante contenant une combinaison d'hinhibiteurs de degradation comportant un derive d'un triazole ou d'un tetrazole et procede d'absorption de composes acides contenus dans un gaz
WO2012125894A2 (fr) * 2011-03-17 2012-09-20 Board Of Regents, The University Of Texas System Inhibiteurs d'oxydation pour la dégradation d'amines

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