WO2015060723A1 - System and process for absorption and desorption of co2 - Google Patents

System and process for absorption and desorption of co2 Download PDF

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Publication number
WO2015060723A1
WO2015060723A1 PCT/NO2013/050178 NO2013050178W WO2015060723A1 WO 2015060723 A1 WO2015060723 A1 WO 2015060723A1 NO 2013050178 W NO2013050178 W NO 2013050178W WO 2015060723 A1 WO2015060723 A1 WO 2015060723A1
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WIPO (PCT)
Prior art keywords
absorption liquid
desorber
droplets
absorber
absorption
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Ceased
Application number
PCT/NO2013/050178
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French (fr)
Inventor
Torbjørn FIVELAND
Henrik Solgaard Andersen
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Equinor Energy AS
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Statoil Petroleum ASA
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Filing date
Publication date
Application filed by Statoil Petroleum ASA filed Critical Statoil Petroleum ASA
Priority to EP13895964.8A priority Critical patent/EP3068510B1/en
Priority to PCT/NO2013/050178 priority patent/WO2015060723A1/en
Publication of WO2015060723A1 publication Critical patent/WO2015060723A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/08—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in rotating vessels; Atomisation on rotating discs
    • 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/24—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 centrifugal force
    • 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
    • B01D2252/20431—Tertiary 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
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20478—Alkanolamines
    • B01D2252/20484—Alkanolamines with one hydroxyl group
    • 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
    • B01D2252/20478—Alkanolamines
    • B01D2252/20489—Alkanolamines with two or more hydroxyl groups
    • 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
    • B01D2252/30—Ionic liquids and zwitter-ions
    • 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
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the present invention relates to a system and a process for absorption and desorption of C0 2 .
  • a standard design of a plant used for carbon dioxide removal from a gas stream such as a flue gas or natural gas comprises a blower either before or after an indirect or direct contact cooler to boost the gas pressure, a separate boiler, followed by a cooler for the gas before the carbon dioxide is removed in an absorption column where the gas is contacted counter-currently to an absorbent flowing downwards.
  • a wash section is fitted to remove, essentially with water, remnants of absorbent following the flue gas from the C0 2 removal section.
  • the known plants and processes for removing C0 2 from a gas stream involve equipment that causes a significant pressure drop in the gas.
  • Absorbent rich in C0 2 from the lower part of the absorber column is pumped to the top of a desorption column via a heat recovery heat exchanger rendering the rich absorbent pre-heated before entering the desorption tower.
  • the absorbent rich in C0 2 is introduced at the top and is stripped by steam moving up the tower. Steam and absorption liquid following C0 2 over the top is recovered in a condenser over the desorber top. Vapour is then formed in a reboiler from where the absorption liquid lean in C0 2 is pumped via a heat recovery heat exchanger and a cooler to the top of the absorption column.
  • a further problem is that there is a lot of energy and heat exchange involved with circulating large amounts of diluted absorbent through the absorption-desorption process.
  • the amount of solution that has to be circulated is highly influenced by the concentration of absorbent that is used in the process. The higher the concentration the less diluent has to be heated, cooled and circulated.
  • the factors that influence the applicable concentration is the viscosity of the solution, the corrosiveness of the solution, the solubility as well as other chemical and physical properties of the solution and the equipment to be used.
  • the object of the present invention is to achieve a system and a process allowing the use of highly concentrated C0 2 absorption liquid in the C0 2 absorption and desorption process.
  • This object is achieved by a system for accelerated absorption and desorption of C0 2 having the features as defined in claim 1.
  • This object is also achieved by the corresponding process for accelerated absorption and desorption of C0 2 having the features as defined in claim 14.
  • the centrifugal effect due to rotation both in the absorber and the desorber it is achieved that the system can handle very viscous solutions.
  • the centrifugal effect improves the efficiency and in both the absorber and the desorber and allows the use of very viscous and highly concentrated absorption liquid.
  • the system is therefore significantly more efficient, up to 30% higher efficiency than conventional plants using standard MEA solutions.
  • the present invention utilizes a high amine concentration, up to 95 % by weight, in particular an amine concentration of approximately 50-70% by weight, and the absorption liquid may have a viscosity of up to 1500 nPa-s.
  • Another advantage is that the retention times of solvents are short in both absorber and desorber and hence the oxidative and thermal degeneration of solvent is also reduced, thus the system and process provides an accelerated absorption and desorption of C0 2 in comparison to previous known processes.
  • Both the absorber and the desorber are very compact and fewer elements are necessary to carry out the absorption of C0 2 and the regeneration of absorption liquid in the desorption process.
  • Another advantage is that since the desorber is operated under pressure, the compressor investments is reduced in comparison to the conventional case. An operating pressure of 5 bara in the desorber gives that one C0 2 compressor stage can be omitted in the plant. The footprint (equipment size) and the investment costs for the system according to the invention is therefore significantly reduced in comparison to previously known plants.
  • the energy consumption for compression compared to standard capture processes amounts to almost 20% reduced energy consumption for an operational pressure of 3 bara, and an energy consumption reduced by almost 30% for an operation pressure of 5 bara in comparison to a design case where the operational pressure is 1.7 bara.
  • Figure 1 schematically illustrates a system according to the invention.
  • FIG. 2 schematically illustrates the absorber in detail.
  • FIG. 3 schematically shows details of the absorber.
  • FIG 4 schematically illustrates the desorber in detail. It should be noted that the figures only show details which are important for the understanding of the invention. Moreover, same features are indicated by the same reference number throughout the specification. It should also be noted that the illustrated apparatus and the features thereof are out of proportion in relation to each other and the indicated features and dimensions thereof are exaggerated. The features are shown in this manner for explanatory purposes only.
  • FIG. 1 a system 1 according to the invention is schematically illustrated.
  • the system shows an absorber 100, also referred to compact atmospheric rotating absorber (CA A) arranged to receive a gas stream 10 such as flue gas or exhaust gas and lean absorption liquid x, also referred to as lean amine, to be used for the absorption process.
  • a desorber 200 also referred to as rotating desorber wheel (RDW 2.0) arranged to receive absorption liquid 3 rich in C0 2 and pressurized steam 4 to be used as heating medium in the desorption process where C02 is desorbed from the C0 2 rich absorption liquid 3 which is regenerated and leaves the desorber as lean absorption liquid 12.
  • the system is further provided with conventional equipment such as compressors, heat exchanger 5 , fans, pumps 6, storage tanks 7,14 , pipes, tubes and fittings and similar to complete the system for the accelerated process of absorption and desorption of C0 2 according to the invention.
  • conventional equipment such as compressors, heat exchanger 5 , fans, pumps 6, storage tanks 7,14 , pipes, tubes and fittings and similar to complete the system for the accelerated process of absorption and desorption of C0 2 according to the invention.
  • the system and process according to the invention allows for using a high amine concentration, up to 95 % by weight, and in particular approximately 50-70% by weight.
  • the present invention is suitable to be used with absorption liquid comprising one of the following MEA, MDEA, DEA, or a mixture of different amines or other absorption liquids such as ionic liquid.
  • Fig. 2 shows the absorber 100 which is provided with a stationary casing 101 having a longitudinal axis and a gas stream inlet 102 and outlet 103.
  • a gas stream 10 containing C0 2 is supplied to the gas stream inlet of the absorber.
  • the casing 101 encloses a rotatable main cylinder 104 which has an absorption section 105 , a demister section 106 and a washing section 107 arranged in series in direction of the gas flow.
  • the mantle surface 108 of the main cylinder functions as the outer perimeter in the radial direction of each section.
  • the absorption section 105 is provided with a plurality of spray means 109 arranged in the centre of the main cylinder.
  • the spray means 109 are arranged to spray absorption liquid 14 into the gas stream 10 in the radial direction towards the perimeter of the main cylinder.
  • the spray means and the perimeter of the main cylinder are means for disintegration 111 of the droplets provided to atomize the droplets and improve the turbulence inside the droplets thereby increasing the absorption efficiency. This is particularly important since the absorption liquid is very viscous and highly concentrated.
  • the droplet disintegration means 111 are formed as a plurality of rotatable cylinders of permeable material, such as densely perforated plates, which are perforated all around the circumference and along the whole length of the cylinder.
  • the perforations 114 are shown in Figure 3.
  • the main cylinder 104 and the perforated cylinders 111 are coaxial and are arranged to rotate about the common longitudinal axis by mechanical driving means 112 of conventional type provided in the absorber.
  • the means for disintegration of droplets comprises 3-50 or more coaxial cylinder which are arranged between the spray means 18 and the mantle surface 11 of the main cylinder.
  • the cylinders are arranged such that the gas stream passes in the axial direction in between the cylinders and is treated by the absorption liquid droplets which are moved in cross-flow direction to the gas stream by aid of the centrifugal effect caused by the rotation of the cylinders.
  • the distance between the cylinders is adapted such that the droplets of absorption liquid are well exposed to the passing gas stream in order to achieve good absorption without blocking or hindering the gas stream.
  • the cylinders 111 are densely perforated such that the droplets pass through the perforations 114 by aid of centrifugal forces without forming a liquid layer on the inside surface of the perforated cylinder.
  • the droplets are atomized and finely divided when passing through the perforations, thus very good mixing inside the droplets is achieved which improves the absorption of C0 2 .
  • the finely atomised absorption liquid droplets provide that large surfaces for mass transfer purpose are exposed to the passing flue gas comprising C0 2 .
  • the average droplet size of absorption liquid decreases with the distance from the centre and the volume of gas between the cylinders increases further out from the hollow axle which allows for high level of absorption of C0 2
  • the absorption liquid collected at the perimeter of the main cylinder is thus rich in C0 2 .
  • the perforated cylinders 111 are attached to the main cylinder 104 by conventional fastening means not shown in the figure but this may easily be done with use of appropriate stays, such that the main cylinder and the inner perforated cylinders rotate together about a common axis.
  • the absorber 100 is further provided with a demister section 106 arranged in the main cylinder directly after the absorption section.
  • the demister section collects and removes remaining droplets of absorption liquid 113 in the treated gas stream 10.
  • the demister is provided with a packed bed material 115, which is arranged to rotate together with the main cylinder.
  • the treated gas stream 10 flows through the packed bed material 115 and droplets of absorption liquid 113 are moved by centrifugal force to the perimeter of the main cylinder.
  • the absorber 100 is further provided with a wash section 107 arranged in the main cylinder directly after the demister section 106.
  • the wash section is arranged like the absorption section and has spray means 109 arranged in the centre for spraying wash liquid 118 into the treated gas stream.
  • the wash section is also provided with means for disintegration of droplets 111 comprising a plurality of rotatable perforated cylinders for atomizing the wash liquid droplets. The droplets are moved by aid of centrifugal force in a cross-flow direction through the gas stream and through the perforated cylinders such that the wash liquid droplets 119 absorb absorption liquid dissolved in the treated gas stream.
  • the absorber 100 is operated at atmospheric pressure. Pressure drop is an important design parameter for atmospheric C0 2 capture. It is therefore preferred to install sufficient pressure generation (fans) at the gas inlet (not shown in the figures) have to overcome pressure drop throughout the absorber.
  • Rich absorption liquid RA is collected at the perimeter of the main cylinder 104 and forms a liquid layer on the inside of the main cylinder surface.
  • the main cylinder is provided with liquid outlets 116 , through holes in the mantle surface 104 where the collected liquid is discharged. The liquid outlets are distributed over the whole main cylinder surface such that both the absorption liquid and the wash liquid is collected and removed via the liquid outlets in respective sections.
  • the liquid outlets 116 arranged on the surface of the main cylinder may optionally be provided with energy recovering means.
  • the energy recovery means comprises diffusers 117 connected to the liquid outlets 116.
  • the diffusers 117 are formed such that the kinetic energy in the liquid layer collected and formed on the inside of the main cylinder is converted into hydrodynamic energy.
  • the diffusers 117 are formed like short tubes with a decreasing cross - section and are directed towards the casing 101 enclosing the main cylinder.
  • the hydrodynamic energy is used as hydrodynamic driving force to rotate the cylinder. This is advantageous in that less power is used by the means for rotating the absorber.
  • the system is further provided with a desorber 200 which is connected to the absorber 100 to receive C0 2 rich absorption liquid.
  • the desorber 200 has a rotatable desorption cylinder 201 which is provided with a desorption chamber 202 and a steam chamber 203.
  • the desorption cylinder 201 is also provided with an absorbent collection chamber 204 for collecting lean absorption liquid 214.
  • the desorption cylinder is rotated by conventional drive means 205 arranged in a suitable manner .
  • the desorption chamber 202 and the steam chamber 203 are integrated in the desorption cylinder 201 to achieve a compact desorber 200. Efficient desorption is achieved without mixing the fluids, thus there is no exchange of substances or mass transfer between the fluids present in the chambers.
  • the chambers are completely separated such that the chambers can be operated with different operating pressures.
  • the system 1 can thus be used with highly pressurized fluids of up to 10 Bar which is advantageous in that energy consumption for desorption is reduced . By using an increased pressure of the released C0 2 the energy consumption for compression in the system 1 is also reduced.
  • the integrated design of the desorption cylinder 201 and the utilisation of centrifugal force created by rotation of the desorption cylinder to force the absorption liquid droplets through the gas stream results in that the desorber is more compact compared to a conventional column and reboiler design.
  • the desorption chamber 202 is provided with spray means 206 in the core region 209 close to the axis of rotation for spraying C0 2 rich absorption liquid 3 into the chamber.
  • the chamber is further provided with a stripper unit 207 arranged between the core region 209 of the chamber and the perimeter 216 of the desorption cylinder 201.
  • the stripper unit 207 is formed as a rotatable tube bundle heat exchanger having a large number of tubes 208 which are attached to the desorption cylinder 201 and rotate together with the cylinder about a rotation axis.
  • the steam chamber 203 is connected to the tubes 208 in the rotating tube bundle heat exchanger 207 such that heated steam 4 is supplied to the inside of the tubes from the steam chamber.
  • the steam condenses in the tubes in the desorption process and the steam condensate 9 is returned via a steam condensate chamber 211 and steam condensate channels 224 (shown in the upper part of the desorption chamber illustrated in Fig. 4 )to the steam chamber.
  • the absorption liquid droplets 212 are sprayed into the core of the desorption chamber 202 and moved by aid of centrifugal force through the tube bundle heat exchanger 207.
  • the desorption process takes place on the outside surface of the tubes 208 where absorption liquid droplets 212 are indirectly heated and releases C0 2 and vapours 13.
  • the desorption cylinder 201 is also provided with an absorbent collection chamber 204 for collecting lean absorption liquid .
  • the lean absorption liquid moves to the periphery 216 of the desorption chamber.
  • Absorbent channels 217 (shown in the lower part of the desorption chamber in Fig. 4) are provided on the perimeter 216 of the desorption chamber and connects the desorption chamber 202 to the absorbent collection chamber 204.
  • the lean absorption liquid 2 is transferred via the absorbent channels 217 to the absorbent collection chamber where the lean absorbent forms a layer 218 on the perimeter of the rotating desorption cylinder.
  • C0 2 and vapours 13 released in the desorption process flows towards the core region 209 of the desorption chamber and preheats the absorption liquid droplets moving outwards.
  • C0 2 is removed from the desorption chamber via an outlet 220 arranged in the core region of the desorption chamber.
  • the absorbent channels 217 and the condensate channels 224 are arranged all around the perimeter of the desorption cylinder.
  • the desorber is provided with means for recovery of kinetic energy in the liquid layer formed on the inside surface of the desorption cylinder in the absorbent collecting chamber 204.
  • the absorbent collection chamber 204 is provided with the diffuser means 221 to remove the lean absorbent from the chamber.
  • the diffuser means are formed of a plurality of stationary diffuser arms, which are connected to a lean absorbent outlet conduit 222 arranged along the axis of rotation of the desorption cylinder.
  • Each diffuser arm 221 is formed like a hollow pipe 223 provided with a liquid inlet arranged in near proximity of the outer perimeter of the absorbent collection chamber.
  • the liquid inlet 228 is funnel shaped and has a cross-section which decreases in the flow direction of the absorbent.
  • the kinetic energy in the rotating layer 218 of the lean absorption liquid 2 is recovered and converted into hydrodynamic energy such as a pressure head.
  • the pressure head has a pumping effect and the liquid is pumped out from the absorbent collection chamber to a storage tank by aid of this pumping effect.
  • the diffuser means By using the diffuser means, at least a part of the supplied energy in order to rotate the desorption cylinder is recovered. Also investments in separate pumps can be avoided.
  • the steam chamber 203 is also provided with diffuser means 221 of the same type as in the absorbent collection chamber 204 for removing steam condensate 9 in the same manner from the desorber.
  • the desorption cylinder 201 is designed such that conduits 230,231 for supplying C0 2 rich absorption liquid 3 and removal of lean absorption liquid 2 are provided in the core region along the axis of rotation of the desorption cylinder, and also the conduit 232 for removing steam condensate 9 from the desorber is provided along the axis of rotation of the desorption cylinder 201.
  • This design decreases the size of the desorber 200 and provides efficient liquid supply and removal systems and demands less energy and investments in pumps and other equipment.
  • the regeneration of the C0 2 rich absorption liquid 3 results in a stream of lean absorption liquid 2 and a gas stream 13 of C0 2 and vapour.
  • the desorber 200 contributes to the steam consumption in the system by use of steam for heating of preheated rich amine to desorption exit temperature, heat for desorption of C0 2 and water vapor leaving the desorber together with C0 2 .
  • Trials indicate that the steam consumption of the desorber amounts to a 30% reduction in steam consumption compared to conventional CO ⁇ capture process cwhich implies less water vapor leaving with the C0 2 .
  • amine solution 70 wt% M EA in water. This will reduce steam consumption needed for C0 2 desorption by almost 30% compared to prior known processes using an amine solution of 30 wt% MEA in water amine.
  • a system 1 according to the invention where the desorber 200 is operated at pressure of 3 bara reduces the compressor energy by almost 20% compared to a desorber of alternative type having operational pressure of 1.7 bara (no compressor steps avoided).
  • the rotating desorber in the system according to the invention is operated at pressure of 5 bara the compressor energy is reduced by almost 30% compared to a desorber of different type having operational pressure of 1.7 bara.
  • the absorption liquid 2, 3 is circulated in the system.
  • the system provides for efficient circulation of the absorption liquid, water, C0 2 , and vapour.
  • Heat exchangers and condensers of different types are used in various process steps for recovering heat and adjusting the operational parameters to achieve high energy efficiency of the system.
  • Rich Amine from the absorber CARA is pumped via a storage tank to the desorber RDW 2.0.
  • the rich amine flow which is fed to the desorber 200 is pre-heated by cooling warm desorbed lean amine 2 coming from the desorber 200, and then heated to desorber operating temperature by steam.
  • the lean amine is further cooled by water to the desired temperature before it is pumped back to the lean amine storage tank 7 of the absorber
  • Warm gases, water vapour and C0 2 , 13 from the gas outlet of the desorber are cooled and water separated in a gas/liquid separator. Energy can be recovered from this stream by condensing of water vapor. Released CO ⁇ is washed with water and is either sent to atmosphere or recycled to increase CO ⁇ concentration in the gas feed.

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

Abstract

The present invention relates to a system 1 for accelerated absorption and desorption of C02 comprising an absorber 100 for absorbing C02 from a gas stream 10 by use of absorption liquid 2 and a desorber 200 for desorbing C02 from C02 rich absorption liquid 3. The absorber 100 comprises a rotatable main cylinder having an absorption section 105 provided with rotatable means for disintegration of droplets 111 of absorption liquid and means for rotating the absorber, such that absorption liquid droplets are moved by aid of centrifugal force in a cross flow-direction in relation to the gas stream and being atomized by the means for disintegration of droplets whereby C02 is absorbed from the gas stream by the absorption liquid droplets. The desorber 200 is connected to the absorber 100 to receive C02 rich absorption liquid 3, and the desorber 200 is rotatable and comprises a desorption chamber 202 provided with a rotatable heat exchanger and means for rotating the desorber, such that the absorption liquid droplets are moved by aid of centrifugal force through the heat exchanger whereby the absorption liquid droplets are heated and C02 is desorbed and separated from the absorption liquid droplets, and lean absorption liquid 2 is circulated to the absorber. The present invention also relates to a process for accelerated absorption and desorption of C02.

Description

System and process for absorption and desorption of C02.
The present invention relates to a system and a process for absorption and desorption of C02.
A standard design of a plant used for carbon dioxide removal from a gas stream such as a flue gas or natural gas comprises a blower either before or after an indirect or direct contact cooler to boost the gas pressure, a separate boiler, followed by a cooler for the gas before the carbon dioxide is removed in an absorption column where the gas is contacted counter-currently to an absorbent flowing downwards. In the top of the column a wash section is fitted to remove, essentially with water, remnants of absorbent following the flue gas from the C02 removal section.
The known plants and processes for removing C02 from a gas stream involve equipment that causes a significant pressure drop in the gas.
Absorbent rich in C02 from the lower part of the absorber column is pumped to the top of a desorption column via a heat recovery heat exchanger rendering the rich absorbent pre-heated before entering the desorption tower. The absorbent rich in C02 is introduced at the top and is stripped by steam moving up the tower. Steam and absorption liquid following C02 over the top is recovered in a condenser over the desorber top. Vapour is then formed in a reboiler from where the absorption liquid lean in C02 is pumped via a heat recovery heat exchanger and a cooler to the top of the absorption column.
Thus, conventional plants consists of very large units comprising a large number of process equipment and require instrumentation and control, in addition to a complex piping system to connect the various units.
A further problem is that there is a lot of energy and heat exchange involved with circulating large amounts of diluted absorbent through the absorption-desorption process. The amount of solution that has to be circulated is highly influenced by the concentration of absorbent that is used in the process. The higher the concentration the less diluent has to be heated, cooled and circulated. The factors that influence the applicable concentration is the viscosity of the solution, the corrosiveness of the solution, the solubility as well as other chemical and physical properties of the solution and the equipment to be used.
The object of the present invention is to achieve a system and a process allowing the use of highly concentrated C02 absorption liquid in the C02 absorption and desorption process. This object is achieved by a system for accelerated absorption and desorption of C02 having the features as defined in claim 1. This object is also achieved by the corresponding process for accelerated absorption and desorption of C02 having the features as defined in claim 14. By using centrifugal effect due to rotation both in the absorber and the desorber it is achieved that the system can handle very viscous solutions. The centrifugal effect improves the efficiency and in both the absorber and the desorber and allows the use of very viscous and highly concentrated absorption liquid. The system is therefore significantly more efficient, up to 30% higher efficiency than conventional plants using standard MEA solutions.
The present invention utilizes a high amine concentration, up to 95 % by weight, in particular an amine concentration of approximately 50-70% by weight, and the absorption liquid may have a viscosity of up to 1500 nPa-s.
This has the further effect that the amounts of circulated absorption liquid are significantly lower, and also the absorption circulation rate is lower. Also the need for heating and cooling large amounts of diluents is therefore reduced.
Another advantage is that the retention times of solvents are short in both absorber and desorber and hence the oxidative and thermal degeneration of solvent is also reduced, thus the system and process provides an accelerated absorption and desorption of C02 in comparison to previous known processes.
Both the absorber and the desorber are very compact and fewer elements are necessary to carry out the absorption of C02 and the regeneration of absorption liquid in the desorption process. Another advantage is that since the desorber is operated under pressure, the compressor investments is reduced in comparison to the conventional case. An operating pressure of 5 bara in the desorber gives that one C02 compressor stage can be omitted in the plant. The footprint (equipment size) and the investment costs for the system according to the invention is therefore significantly reduced in comparison to previously known plants.
Furthermore, the energy consumption for compression compared to standard capture processes (depending on the operational pressure in the desorber) amounts to almost 20% reduced energy consumption for an operational pressure of 3 bara, and an energy consumption reduced by almost 30% for an operation pressure of 5 bara in comparison to a design case where the operational pressure is 1.7 bara.
Other distinctive features and advantages with the invention will be evident in the dependent claims and the following detailed description of preferred embodiments of the invention.
Figure 1 schematically illustrates a system according to the invention.
Figure 2 schematically illustrates the absorber in detail.
Figure 3 schematically shows details of the absorber.
Figure 4 schematically illustrates the desorber in detail. It should be noted that the figures only show details which are important for the understanding of the invention. Moreover, same features are indicated by the same reference number throughout the specification. It should also be noted that the illustrated apparatus and the features thereof are out of proportion in relation to each other and the indicated features and dimensions thereof are exaggerated. The features are shown in this manner for explanatory purposes only.
With reference to figure 1 a system 1 according to the invention is schematically illustrated.
The system shows an absorber 100, also referred to compact atmospheric rotating absorber (CA A) arranged to receive a gas stream 10 such as flue gas or exhaust gas and lean absorption liquid x, also referred to as lean amine, to be used for the absorption process. A desorber 200 , also referred to as rotating desorber wheel (RDW 2.0) arranged to receive absorption liquid 3 rich in C02 and pressurized steam 4 to be used as heating medium in the desorption process where C02 is desorbed from the C02 rich absorption liquid 3 which is regenerated and leaves the desorber as lean absorption liquid 12. The system is further provided with conventional equipment such as compressors, heat exchanger 5 , fans, pumps 6, storage tanks 7,14 , pipes, tubes and fittings and similar to complete the system for the accelerated process of absorption and desorption of C02 according to the invention. These types of equipments are previously known and therefore not further described here.
The system and process according to the invention allows for using a high amine concentration, up to 95 % by weight, and in particular approximately 50-70% by weight. The present invention is suitable to be used with absorption liquid comprising one of the following MEA, MDEA, DEA, or a mixture of different amines or other absorption liquids such as ionic liquid.
Fig. 2 shows the absorber 100 which is provided with a stationary casing 101 having a longitudinal axis and a gas stream inlet 102 and outlet 103. A gas stream 10 containing C02 is supplied to the gas stream inlet of the absorber.
The casing 101 encloses a rotatable main cylinder 104 which has an absorption section 105 , a demister section 106 and a washing section 107 arranged in series in direction of the gas flow. The mantle surface 108 of the main cylinder functions as the outer perimeter in the radial direction of each section. The absorption section 105 is provided with a plurality of spray means 109 arranged in the centre of the main cylinder. The spray means 109 are arranged to spray absorption liquid 14 into the gas stream 10 in the radial direction towards the perimeter of the main cylinder. Between the spray means and the perimeter of the main cylinder are means for disintegration 111 of the droplets provided to atomize the droplets and improve the turbulence inside the droplets thereby increasing the absorption efficiency. This is particularly important since the absorption liquid is very viscous and highly concentrated.
The droplet disintegration means 111 are formed as a plurality of rotatable cylinders of permeable material, such as densely perforated plates, which are perforated all around the circumference and along the whole length of the cylinder. The perforations 114 are shown in Figure 3. The main cylinder 104 and the perforated cylinders 111 are coaxial and are arranged to rotate about the common longitudinal axis by mechanical driving means 112 of conventional type provided in the absorber. The means for disintegration of droplets comprises 3-50 or more coaxial cylinder which are arranged between the spray means 18 and the mantle surface 11 of the main cylinder. The cylinders are arranged such that the gas stream passes in the axial direction in between the cylinders and is treated by the absorption liquid droplets which are moved in cross-flow direction to the gas stream by aid of the centrifugal effect caused by the rotation of the cylinders. The distance between the cylinders is adapted such that the droplets of absorption liquid are well exposed to the passing gas stream in order to achieve good absorption without blocking or hindering the gas stream. The cylinders 111 are densely perforated such that the droplets pass through the perforations 114 by aid of centrifugal forces without forming a liquid layer on the inside surface of the perforated cylinder. Since the perforated cylinders rotate together with the main cylinder, the droplets are atomized and finely divided when passing through the perforations, thus very good mixing inside the droplets is achieved which improves the absorption of C02. The finely atomised absorption liquid droplets provide that large surfaces for mass transfer purpose are exposed to the passing flue gas comprising C02.
The average droplet size of absorption liquid decreases with the distance from the centre and the volume of gas between the cylinders increases further out from the hollow axle which allows for high level of absorption of C02 The absorption liquid collected at the perimeter of the main cylinder is thus rich in C02.
The perforated cylinders 111 are attached to the main cylinder 104 by conventional fastening means not shown in the figure but this may easily be done with use of appropriate stays, such that the main cylinder and the inner perforated cylinders rotate together about a common axis. The absorber 100 is further provided with a demister section 106 arranged in the main cylinder directly after the absorption section. The demister section collects and removes remaining droplets of absorption liquid 113 in the treated gas stream 10. The demister is provided with a packed bed material 115, which is arranged to rotate together with the main cylinder. The treated gas stream 10 flows through the packed bed material 115 and droplets of absorption liquid 113 are moved by centrifugal force to the perimeter of the main cylinder.
The absorber 100 is further provided with a wash section 107 arranged in the main cylinder directly after the demister section 106. The wash section is arranged like the absorption section and has spray means 109 arranged in the centre for spraying wash liquid 118 into the treated gas stream. The wash section is also provided with means for disintegration of droplets 111 comprising a plurality of rotatable perforated cylinders for atomizing the wash liquid droplets. The droplets are moved by aid of centrifugal force in a cross-flow direction through the gas stream and through the perforated cylinders such that the wash liquid droplets 119 absorb absorption liquid dissolved in the treated gas stream. Optionally, there is also a further demister section arranged after the wash section such that all wash liquid is removed from the cleaned gas before the gas vented to the atmosphere. The absorber 100 is operated at atmospheric pressure. Pressure drop is an important design parameter for atmospheric C02 capture. It is therefore preferred to install sufficient pressure generation (fans) at the gas inlet (not shown in the figures) have to overcome pressure drop throughout the absorber. Rich absorption liquid RA, is collected at the perimeter of the main cylinder 104 and forms a liquid layer on the inside of the main cylinder surface. The main cylinder is provided with liquid outlets 116 , through holes in the mantle surface 104 where the collected liquid is discharged. The liquid outlets are distributed over the whole main cylinder surface such that both the absorption liquid and the wash liquid is collected and removed via the liquid outlets in respective sections.
The liquid outlets 116 arranged on the surface of the main cylinder may optionally be provided with energy recovering means. The energy recovery means comprises diffusers 117 connected to the liquid outlets 116. The diffusers 117 are formed such that the kinetic energy in the liquid layer collected and formed on the inside of the main cylinder is converted into hydrodynamic energy. The diffusers 117 are formed like short tubes with a decreasing cross - section and are directed towards the casing 101 enclosing the main cylinder. The hydrodynamic energy is used as hydrodynamic driving force to rotate the cylinder. This is advantageous in that less power is used by the means for rotating the absorber.
The system is further provided with a desorber 200 which is connected to the absorber 100 to receive C02 rich absorption liquid. The desorber 200 has a rotatable desorption cylinder 201 which is provided with a desorption chamber 202 and a steam chamber 203. The desorption cylinder 201 is also provided with an absorbent collection chamber 204 for collecting lean absorption liquid 214. The desorption cylinder is rotated by conventional drive means 205 arranged in a suitable manner .
The desorption chamber 202 and the steam chamber 203 are integrated in the desorption cylinder 201 to achieve a compact desorber 200. Efficient desorption is achieved without mixing the fluids, thus there is no exchange of substances or mass transfer between the fluids present in the chambers. The chambers are completely separated such that the chambers can be operated with different operating pressures. The system 1 can thus be used with highly pressurized fluids of up to 10 Bar which is advantageous in that energy consumption for desorption is reduced . By using an increased pressure of the released C02 the energy consumption for compression in the system 1 is also reduced. The integrated design of the desorption cylinder 201 and the utilisation of centrifugal force created by rotation of the desorption cylinder to force the absorption liquid droplets through the gas stream results in that the desorber is more compact compared to a conventional column and reboiler design.
The desorption chamber 202 is provided with spray means 206 in the core region 209 close to the axis of rotation for spraying C02 rich absorption liquid 3 into the chamber. The chamber is further provided with a stripper unit 207 arranged between the core region 209 of the chamber and the perimeter 216 of the desorption cylinder 201.
The stripper unit 207 is formed as a rotatable tube bundle heat exchanger having a large number of tubes 208 which are attached to the desorption cylinder 201 and rotate together with the cylinder about a rotation axis.
The steam chamber 203 is connected to the tubes 208 in the rotating tube bundle heat exchanger 207 such that heated steam 4 is supplied to the inside of the tubes from the steam chamber. The steam condenses in the tubes in the desorption process and the steam condensate 9 is returned via a steam condensate chamber 211 and steam condensate channels 224 (shown in the upper part of the desorption chamber illustrated in Fig. 4 )to the steam chamber.
The absorption liquid droplets 212 are sprayed into the core of the desorption chamber 202 and moved by aid of centrifugal force through the tube bundle heat exchanger 207. The desorption process takes place on the outside surface of the tubes 208 where absorption liquid droplets 212 are indirectly heated and releases C02 and vapours 13. The desorption cylinder 201 is also provided with an absorbent collection chamber 204 for collecting lean absorption liquid . The lean absorption liquid moves to the periphery 216 of the desorption chamber. Absorbent channels 217 (shown in the lower part of the desorption chamber in Fig. 4) are provided on the perimeter 216 of the desorption chamber and connects the desorption chamber 202 to the absorbent collection chamber 204. The lean absorption liquid 2 is transferred via the absorbent channels 217 to the absorbent collection chamber where the lean absorbent forms a layer 218 on the perimeter of the rotating desorption cylinder. C02 and vapours 13 released in the desorption process flows towards the core region 209 of the desorption chamber and preheats the absorption liquid droplets moving outwards. C02 is removed from the desorption chamber via an outlet 220 arranged in the core region of the desorption chamber.
The absorbent channels 217 and the condensate channels 224 are arranged all around the perimeter of the desorption cylinder. The desorber is provided with means for recovery of kinetic energy in the liquid layer formed on the inside surface of the desorption cylinder in the absorbent collecting chamber 204. The absorbent collection chamber 204 is provided with the diffuser means 221 to remove the lean absorbent from the chamber. The diffuser means are formed of a plurality of stationary diffuser arms, which are connected to a lean absorbent outlet conduit 222 arranged along the axis of rotation of the desorption cylinder. Each diffuser arm 221 is formed like a hollow pipe 223 provided with a liquid inlet arranged in near proximity of the outer perimeter of the absorbent collection chamber. The liquid inlet 228 is funnel shaped and has a cross-section which decreases in the flow direction of the absorbent. The kinetic energy in the rotating layer 218 of the lean absorption liquid 2 is recovered and converted into hydrodynamic energy such as a pressure head. The pressure head has a pumping effect and the liquid is pumped out from the absorbent collection chamber to a storage tank by aid of this pumping effect. By using the diffuser means, at least a part of the supplied energy in order to rotate the desorption cylinder is recovered. Also investments in separate pumps can be avoided. The steam chamber 203 is also provided with diffuser means 221 of the same type as in the absorbent collection chamber 204 for removing steam condensate 9 in the same manner from the desorber.
The desorption cylinder 201 is designed such that conduits 230,231 for supplying C02 rich absorption liquid 3 and removal of lean absorption liquid 2 are provided in the core region along the axis of rotation of the desorption cylinder, and also the conduit 232 for removing steam condensate 9 from the desorber is provided along the axis of rotation of the desorption cylinder 201. This design decreases the size of the desorber 200 and provides efficient liquid supply and removal systems and demands less energy and investments in pumps and other equipment. The regeneration of the C02 rich absorption liquid 3 results in a stream of lean absorption liquid 2 and a gas stream 13 of C02 and vapour.
The desorber 200 contributes to the steam consumption in the system by use of steam for heating of preheated rich amine to desorption exit temperature, heat for desorption of C02 and water vapor leaving the desorber together with C02. Trials indicate that the steam consumption of the desorber amounts to a 30% reduction in steam consumption compared to conventional CO^ capture process cwhich implies less water vapor leaving with the C02. It should be noted that there is significantly reduced energy consumption for amine desorption due to compact equipment design and the use of highly concentrated absorption liquid, amine solution (70 wt% M EA in water). This will reduce steam consumption needed for C02 desorption by almost 30% compared to prior known processes using an amine solution of 30 wt% MEA in water amine.
Furthermore it should be noted that the operational pressure of the rotating desorber in the system can be significantly higher than for known desorption alternatives, due to the design of the system and the design of the desorber. Hence C02 compressor energy consumption post the desorption process and the subsequent pressurisation to the required level of 70 bar is less than for alternative strippers.
Furthermore, a system 1 according to the invention where the desorber 200 is operated at pressure of 3 bara reduces the compressor energy by almost 20% compared to a desorber of alternative type having operational pressure of 1.7 bara (no compressor steps avoided). In case the rotating desorber in the system according to the invention is operated at pressure of 5 bara the compressor energy is reduced by almost 30% compared to a desorber of different type having operational pressure of 1.7 bara.
The absorption liquid 2, 3 is circulated in the system. The system provides for efficient circulation of the absorption liquid, water, C02, and vapour. Heat exchangers and condensers of different types are used in various process steps for recovering heat and adjusting the operational parameters to achieve high energy efficiency of the system. Rich Amine from the absorber CARA is pumped via a storage tank to the desorber RDW 2.0. The rich amine flow which is fed to the desorber 200 is pre-heated by cooling warm desorbed lean amine 2 coming from the desorber 200, and then heated to desorber operating temperature by steam. The lean amine is further cooled by water to the desired temperature before it is pumped back to the lean amine storage tank 7 of the absorber
Warm gases, water vapour and C02, 13 from the gas outlet of the desorber are cooled and water separated in a gas/liquid separator. Energy can be recovered from this stream by condensing of water vapor. Released CO^ is washed with water and is either sent to atmosphere or recycled to increase CO^ concentration in the gas feed.

Claims

Claims
1. System for accelerated absorption and desorption of C02 comprising an absorber (100) for absorbing C02 from a gas stream (10) by use of absorption liquid and a desorber (200) for desorbing C02 from C02 rich absorption liquid, characterized in that the absorber (100) comprises a rotatable main cylinder (104) having an absorption section (105) provided with rotatable means for disintegration of droplets (111) of absorption liquid and means for rotating (112) the absorber, such that absorption liquid droplets (113) are moved by aid of centrifugal force in a cross flow-direction in relation to the gas stream (10) and being atomized by the means for disintegration of droplets whereby C02 is absorbed from the gas stream by the absorption liquid droplets, the desorber (200) is connected to the absorber to receive C02 rich absorption liquid, the desorber (200) is rotatable and comprises a desorption chamber (202) provided with a rotatable heat exchanger (207) and means for rotating (205) the desorber, such that the absorption liquid droplets (212) are moved by aid of centrifugal force through the heat exchanger (207) whereby the absorption liquid droplets are heated and C02 is desorbed and separated from the absorption liquid droplets, and lean absorption liquid is circulated to the absorber (100).
2. System according to claim 1, wherein the means for disintegration of droplets (111) comprises a plurality of perforated rotating cylinders.
3. System according to any of previous claims wherein the absorber (100) is provided with means for recovery of kinetic energy (117) in the absorption liquid.
4. System according to claim 3 wherein the main cylinder (104) is provided with diffusers (117) connected to liquid outlets (116) arranged on the mantle surface to convert kinetic energy in the C02 rich absorption liquid (3) into hydrodynamic energy.
5. System according to any of previous claims wherein the desorber is provided with means for recovery of kinetic energy (221) in the lean absorption liquid (2) and/or steam condensate (9) .
6. System according to claim 5 wherein the desorber is provided with stationary diffusers (221) arranged in an absorbent collection chamber (204) to convert kinetic energy in lean absorption liquid (2) into hydrodynamic energy.
7. System according to claim 5 or 6 wherein the desorber is provided with stationary diffusers (221) arranged in a steam chamber (203) to convert kinetic energy in steam condensate (9) into hydrodynamic energy.
8. System according to any the previous claims wherein the main cylinder of the absorber has a demister section (106) arranged after the absorption section (105) which is adapted to remove droplets of absorption liquid (113) from the treated gas stream.
9. System according to any the previous claims wherein the main cylinder (104) of the absorber has a wash section (107) arranged after the demister section where wash liquid (118) is sprayed into the gas stream, and provided with means for disintegration of droplets (111), and the wash liquid droplets (119) are moved by aid of centrifugal force in a cross-flow direction in relation to the gas stream whereby the wash liquid droplets absorb absorption liquid dissolved in the treated gas stream.
10. System according to any the previous claims wherein the main cylinder (104) of the absorber is provided with a demister section (105) which is arranged after the wash section (107), and the demister section adapted for removing droplets of wash liquid from the treated gas stream.
11. System according to any the previous claims wherein the desorber (200) comprises a steam chamber (203), and that the desorption chamber (202) and the steam chamber (203) are arranged such that absorption liquid (2,3) in the desorption chamber (202) and heating medium (4,9) in the steam chamber are not mixed in the desorber.
12. System according to any the previous claims wherein absorption liquid (2,3) is supplied and removed from the desorber along the axis of rotation of the desorption cylinder.
13. System according to any the previous claims wherein steam condensate (9) is removed from the desorber along the axis of rotation of the desorption cylinder.
14. Process for accelerated absorption and desorption of C02 comprising the steps
-supplying a gas stream (10) containing C02 to an absorber (100) having a rotating main cylinder (104), -spraying lean absorption liquid (110) into the gas stream, -moving absorption liquid droplets (113) in a cross-flow direction to the gas stream by aid of centrifugal force,
-atomizing the droplets of absorption liquid (113) by means for disintegration of droplets (111) ,
-absorbing C02 from the gas stream (10) by absorption liquid droplets(113), -circulating C02 rich absorption liquid (3) from the absorber to a rotating desorber (200) having a desorption chamber (202) provided with a rotating heat exchanger (207),
-spraying C02 rich absorption liquid in the desorption chamber (202),
-supplying steam (4)to the heat exchanger,
-moving droplets of absorption liquid (212) through heat exchanger (207) by aid of centrifugal force, -desorbing C02 from absorption liquid,
-separating C02 from lean absorption liquid,
-circulating lean absorption liquid (2) from the desorber (200) to the absorber (100).
15. Process according to claim 14 comprising recovering kinetic energy from the absorption liquid in the absorber.
16. Process according to claim 15 comprising converting kinetic energy in the absorption liquid to hydrodynamic energy.
17. Process according to any of claims 14-16 comprising recovering kinetic energy from the absorption liquid (2) in the desorber.
18. Process according to any one of claims 14-17 comprising recovering kinetic energy from steam condensate (9) in the desorber.
19. Process according to any one of claims 14-18 comprising pressurizing the steam chamber (203) and/or the desorption chamber (202) in operation.
20. Process according to any one of claims 14-19 wherein the absorption liquid has an amine concentration up to 95 % by weight.
21. Process according to any one of the claims 14-20 wherein the absorption liquid has an amine concentration of approximately 50-70% by weight.
22. Process according to any one of claims 14-21 wherein the absorption liquid has viscosity of up to 1500 nPa-s.
23. Process according to any one of claims 14-22 wherein the absorption liquid comprises one of the following MEA, MDEA, DEA, or a mixture of different amines or other absorption liquids such as ionic liquid.
PCT/NO2013/050178 2013-10-22 2013-10-22 System and process for absorption and desorption of co2 Ceased WO2015060723A1 (en)

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