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WO2008153379A1 - Procédé et dispositif pour séparer le co2 d'un mélange de gaz de combustion ou de gaz de synthèse provenant de procédés de conversion de combustibles fossiles et de biocombustibles - Google Patents

Procédé et dispositif pour séparer le co2 d'un mélange de gaz de combustion ou de gaz de synthèse provenant de procédés de conversion de combustibles fossiles et de biocombustibles Download PDF

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Publication number
WO2008153379A1
WO2008153379A1 PCT/NL2008/050323 NL2008050323W WO2008153379A1 WO 2008153379 A1 WO2008153379 A1 WO 2008153379A1 NL 2008050323 W NL2008050323 W NL 2008050323W WO 2008153379 A1 WO2008153379 A1 WO 2008153379A1
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Prior art keywords
gas mixture
mixture
gas
temperature
fraction
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Application number
PCT/NL2008/050323
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English (en)
Inventor
Raichel Elton Taciano Leito
Jozef Johannes Hubertus Brouwers
Original Assignee
Romico Hold A.V.V.
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Filing date
Publication date
Application filed by Romico Hold A.V.V. filed Critical Romico Hold A.V.V.
Publication of WO2008153379A1 publication Critical patent/WO2008153379A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
    • B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
    • B01D45/14—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces generated by rotating vanes, discs, drums or brushes
    • 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
    • B01D53/002—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 condensation
    • 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
    • B01D53/22—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 diffusion
    • B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
    • 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
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/408—Cyanides, e.g. hydrogen cyanide (HCH)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • 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 method and device for separating CO 2 and optionally other substances from a flue gas or synthesis gas mixture from fossil and biomass-fuelled processes.
  • Flue gases and synthesis gases are created in respectively the combustion and the chemical conversion of fossil and biomass fuels. Synthesis gases are increasingly applied in, among others, the chemical industry, for instance as power supply.
  • harmful gases such as for instance the greenhouse gas CO 2 .
  • CO 2 the greenhouse gas
  • ratification of the Kyoto Protocol additional obligations have been imposed on many countries to reduce the emission of greenhouse gases, and CO 2 in particular. It is to be expected that the threat of climate change will result in even more stringent requirements in respect of this emission. For this and other reasons the energy market is in a state of great turmoil at the moment. Coal is thus for instance gaining importance again as a fossil fuel. Because of the competitive cost price of coal compared to other fossil fuels, growth economies such as China and India are at the moment making massive investment in the construction of new coal-fired power plants.
  • the use of fossil fuels has drawbacks.
  • the flue gases of classic coal-fired power plants contain high concentrations of SO ⁇ , NO ⁇ , soot particles and dust particles.
  • large quantities of CO 2 are generally released in the combustion of fossil fuels. Technologies have meanwhile become available for the removal of SO ⁇ , NO x , soot particles and dust particles.
  • the so-called Integrated Gasification Combined Cycle (IGCC) technology has thus been developed, wherein the coal is not combusted but is converted into so-called synthesis gas at high pressure and temperature via a gasification process.
  • the synthesis gas comprises on average about 30 mol% H 2 , 65 mol% CO, 3 mol% N 2 , 1 mol% H 2 O and 1 mol% CO 2 .
  • the contaminants are removed from the synthesis gas by cooling it to a temperature in the order of magnitude of 10O 0 C, wherein steam is produced.
  • the sulphur, nitrogen and soot particles are then removed with the usual low-temperature techniques.
  • the separation OfCO 2 from flue gases and/or synthesis gases has heretofore been found to be time-consuming.
  • IGCC for instance a decarbonization of the synthesis gas is performed. CO from the synthesis gas is converted with steam via a so-called CO-shift reaction into a gas mixture comprising H 2 and CO 2 (wherein several mol% N 2 may also be present). A gas mixture with a high concentration of CO 2 is thus obtained.
  • a gas mixture of 40-50 mol% H 2 , 40-50 mol% CO 2 and several mol% N 2 is typical.
  • a physical adsorption technique is then applied thereto using membranes. Physical separation techniques are less economic, certainly when processing large volumes of gas mixture. It has moreover been found that when membrane technology is used the total CO 2 recovery is generally no higher than between 50% and 75% of the quantity present. The recovered CO 2 is further often impure, wherein more than 5 mol% of other molecules are present in the recovered CO 2 mixture.
  • the membrane technology is also expensive, among other reasons because it consumes a great deal of energy. In addition, operation usually takes place in multiple steps in the known membrane separation, wherein the gas mixture for purifying must be guided through a cascade of membranes in order to obtain a fraction with high purity.
  • the present invention has for its object to provide a method and device for separating CO? from a gas mixture which has an increased selectivity for the CO 2 to be separated, and which also enables a rapid separation.
  • the invention provides for this purpose a method as according to the preamble, which is further characterized in that it comprises the processing steps of:
  • WO 2005/11811OA a method for separating a medium mixture into fractions.
  • a medium mixture is provided which is cooled to a final temperature and a final pressure at which at least one of the fractions present is present at least partially in the liquid phase in the medium mixture.
  • the thus resulting medium mixture is subjected to a volume force, wherein separation occurs.
  • the separated fractions are then discharged.
  • WO 2005/1 1811OA describes an example in which a contaminated natural gas is purified of, among other gases, CO 2 . It cannot be inferred from WO 2005/1181 1OA that the method described therein is specifically suitable for separating CO 2 from flue gas or synthesis gas mixtures from fossil and biomass-fuelled processes. Such gases do after all originally contain no CO?, or only a small quantity thereof.
  • the gas mixture is cooled to a final temperature at which the CO 2 is present at least partially, and more preferably substantially wholly, in the liquid phase in the gas mixture.
  • the separated CO 2 fraction is liquid and can moreover have a high degree of purity, this fraction can be readily pumped over relatively large distances.
  • the pumping of the liquid CO 2 fraction can take place with little energy loss, wherein the temperature is moreover easily held at the desired low level.
  • a further advantage of the method according to the present invention is that the energy consumption thereof is exceptionally low.
  • a C ⁇ 2 -containing flue gas or synthesis gas mixture from fossil and biomass-fuelled processes is provided by converting CO from a flue gas or synthesis gas by means of a CO-shift reaction with steam.
  • a gas mixture is thus obtained with a high concentration of CO 2 , from which the CO 2 can be separated with high efficiency.
  • the present invention can further be applied for separating other substances (in addition to CO 2 ) possibly present in the gas mixture.
  • a gas mixture is thus obtained of at least CO 2 and the notorious hydrogen cyanide gas (HCN).
  • HCN notorious hydrogen cyanide gas
  • metallurgical deposition can also comprise heavy metals such as for instance cadmium, mercury, lead and zinc.
  • Existing gas treatment methods such as the known scrubbing of contaminants (wet gas scrubbing) are often found to be time- consuming and economically not sufficiently cost-effective.
  • the method according to the invention is then preferably characterized in that the gas mixture is cooled to a final temperature at which the HCN is present substantially in the liquid phase in the gas mixture.
  • the CO 2 present in the gas mixture will preferably be in the gas phase at this final temperature. It is not therefore necessary according to the invention for the CO 2 to be in the gas phase during step C) of the method, this can also be a different fraction of the gas mixture.
  • the temperature decrease to the final temperature can for instance be achieved by feeding the gas to active or passive cooling means. Although not essential according to the invention, it is advantageous when the temperature is reduced isobarically, therefore at almost constant pressure. Because the temperature is reduced according to the invention to below the temperature at which at least a part of at least one of the fractions present in the gas mixture is liquid, the gas mixture as a whole will undergo a phase separation. By cooling the gas mixture before starting the separation at least one of the fractions present in the gas mixture, and preferably the CO 2 fraction, will undergo a phase change from gas to liquid, wherein possible other constituents remain in the gaseous phase. A medium mixture is in this way created with a gaseous matrix incorporating liquid droplets. It has been found that CO 2 can be can be separated with increased selectivity from such a mixture.
  • the cooling and/or the expansion is performed such that the final temperature is a maximum of 50 0 C higher than the temperature which at the final pressure corresponds to the transition of the at least one fraction to the solid phase.
  • the final temperature is more preferably a maximum of 20 0 C higher than the temperature which at the final pressure corresponds to the transition of the at least one fraction to the solid phase.
  • the at least one fraction is the CO 2 fraction. In such a preferred embodiment wherein the at least one fraction is the CO 2 fraction, it is advantageous that the final temperature lies between -80 0 C and -20 0 C, and the final pressure between 10 and 80 Bar.
  • the choice of the final temperature is still more preferably between -60 0 C and -4O 0 C, and the final pressure between 20 and 60 Bar, and most preferably between -50 0 C and -40 0 C and between 30 and 60 Bar.
  • the at least one fraction is the HCN fraction
  • the choice of the final temperature is most preferably between 0 0 C and 4O 0 C, and the final pressure between 5 and 30 Bar.
  • a phase diagram of the gas mixture (a diagram of the pressure against the temperature) is generally characterized by a range where the fractions of the gas mixture form one phase (the mixing range) and a more or less closed range where at least a part of the fractions form a distinct phase (demixing range).
  • a gaseous range, a liquid range and a solid range are generally further distinguished, wherein the gaseous range is located on average at high pressure and temperature and the solid range, conversely, at low pressure and temperature.
  • a number of lines demarcate these ranges, in particular a liquid line which indicates the boundary between combinations of pressure and temperature under which (in addition to other phases) a liquid phase also occurs, and a solid line which indicates the boundary between combinations of pressure and temperature under which (in addition to other phases) a solid phase also occurs.
  • the temperature which at the final pressure corresponds to the transition of the at least one fraction to substantially solid phase is thus the temperature as according to the intersection of the final pressure line and the solid line for the relevant phase.
  • the separation efficiency of the rotation means is increased according to the present invention by bringing at least one fraction, and preferably the CO 2 fraction, at least partially and preferably substantially into liquid form before the gas mixture reaches the rotation means. This phase change takes place by changing the temperature (heating or cooling subject to the conditions) and/or the pressure of the gas mixture.
  • the separation of the fractions is understood to mean at least partial separation of two fractions such that a significant difference in the average mass density of the two fractions results; a complete (100%) separation will be difficult to realize in practice.
  • the lighter fraction will migrate at least substantially to the inner side of the rotation and the heavier fraction (the liquid fraction) will migrate at least substantially to the outer side of the rotation.
  • the present invention relates to a separation which moreover increases the possible uses of at least one of the fractions compared to the gas mixture. Even after separation, this usable ("cleaned") fraction may still comprise a part of another undesired fraction (be contaminated with another fraction), although this other fraction will be significantly smaller than the presence of this undesired fraction in the original mixture.
  • the usable fraction will comprise an H 2 - containing gas mixture.
  • the successive steps of the method according to the invention result in an unexpectedly high separation efficiency without bulky equipment being required for this purpose (i.e. the device can be given a very compact form) and wherein the medium need only be treated for a short period.
  • a device can be given an even smaller form (with a smaller volume) if the medium mixture is carried under higher pressure through the device.
  • the medium mixture is subjected to gravitational force during processing step C).
  • Such a separation technique is very simple and requires little energy and investment.
  • the medium mixture is subjected to a centrifugal force during processing step C) by feeding the medium mixture to rotation means.
  • the rotation means can for instance be formed by at least one cyclone (vortex), or alternatively by an assembly of a plurality of cyclones.
  • a cyclone it is possible to give the rotation means a stationary form and to set only the medium into rotation.
  • the application of a plurality of (smaller) cyclones has an advantage relative to a single cyclone which is comparable to the advantage of a rotating assembly of feed channels.
  • Baffles can optionally be placed in a cyclone, for instance for the purpose of causing a determined fraction to condense on the baffles and for controlling the cyclone.
  • a particularly favourable method according to the invention is characterized in that during processing step C) the medium mixture is set into rotating flow in rotation means provided for this purpose and comprising a rotating assembly of feed channels.
  • Such rotary separators have the advantage that the average distance of the medium from a wall (in radial direction) remains limited, whereby a desired degree of separation can be achieved in a relatively short time (which corresponds to a relatively limited length of the rotary separator in axial direction).
  • the operation of such a rotating assembly of feed channels is further influenced positively if a preferably laminar flow of the medium is maintained in the channels.
  • the medium to be carried through the channels with turbulent flow.
  • the flow speeds to be applied can be varied or optimized according to the situation.
  • a particularly suitable rotary separator of the present type is described for instance in EP 0286160A, the content of which is expressly incorporated in the present application.
  • the method according to the invention is applied by subjecting the medium mixture during processing step C) to gravitational force and/or to a centrifugal force, and/or setting the medium mixture into rotating flow in rotation means provided for this purpose and comprising a rotating assembly of feed channels.
  • the combination of separating techniques can result in a further increased selectivity of the CO 2 to be separated from the gas mixture.
  • the separated gaseous fraction is further purified by being guided downstream of the rotation means through at least one membrane (physical adsorption) and/or through a washer (chemical absorption). This has the additional advantage that the selectivity is further improved, particularly also because physical adsorption and/or chemical absorption separation consumes less energy the lower the CO 2 content in the gas mixture becomes.
  • the method according to the invention can be performed with a relatively small throughflow device since the separate processing steps can be carried out within a very short period of time, for instance individually in less than 1 second, usually in less than 0.1 second or even in less than 10 or less than 5 milliseconds. This makes lengthy processes, with associated devices which are dimensioned such that they can contain large volumes, unnecessary.
  • the method according to the invention is applied particularly for the purpose of separating CO 2 from a flue gas and/or synthesis gas of a fossil and/or biomass-fuelled process.
  • the method is then characterized in that a flue gas and/or synthesis gas of a fossil and/or biomass-fuelled process is provided during processing step A).
  • the CO 2 can be separated from the gas mixture with high selectivity.
  • This particularly favourable effect is achieved, among other ways, by bringing at least one of the fractions present in the gas mixture, and preferably the CO 2 fraction, at least partially into liquid form prior to the actual separation, whereby a phase separation occurs in the gas mixture.
  • the method according to the invention has the additional advantage that the liquid fraction can be discharged in step D) by being pumped. If this liquid fraction is the CO 2 fraction, the separated CO 2 can then be transported in very simple manner to a location where it can be stored. This is preferably a location on the seabed. The separated CO 2 can in this way also be carried to an underground reservoir of porous rock. Storage on the seabed can make a significant contribution to the solution of the greenhouse problem. It is noted that a location on the seabed is understood to mean any location deep enough below sea level to allow for instance CO 2 to easily dissolve in the seawater.
  • the invention also relates to a device for separating CO 2 from a gas mixture, the operation and advantages of which have already been elucidated at length above in respect of the method.
  • the device comprises: - rotation means for rotating the flowing gas mixture to be separated, a cooling and/or expansion means, connecting to the rotation means upstream in flow direction of the gas mixture, for causing transition in physical manner of at least one of the fractions present in the gas mixture to the liquid phase, a feed for the medium mixture to be separated connecting to the cooling and/or expansion means, and pump means connecting to the rotation means for discharging the separated liquid phase.
  • the rotation means are preferably formed by a rotating assembly of feed channels and/or by at least one cyclone. It is further advantageous to characterize the device in that the pump means connect to a location on the seabed and/or underground reservoir of porous rock.
  • range G the medium mixture is gaseous
  • range G+L a mixture is present of liquid and gas, wherein in the present case CO 2 is in the liquid phase and the rest of the components in the gaseous phase.
  • Present in range G+S+L is a mixture of gas, liquid and solid.
  • a number of lines demarcate the relevant ranges, in particular a dew point line 1 10 which indicates the boundary between combinations of pressure 100 and temperature 200 below which (in addition to other phases) a liquid phase L also occurs, and a solid line 120 which indicates the boundary between combinations of pressure 100 and temperature 200 below which (in addition to other phases) a solid phase VS also occurs. It will be apparent that the phase diagram shown in figure 2 is given only by way of example, and that the method is likewise applicable for separating CO 2 - containing gas mixtures with more fractions, and therefore a more complicated phase diagram.
  • Figure 3 thus shows a phase diagram of a synthesis gas which can be cleaned with the invented method. This is more particularly the phase diagram of a 50/50 mol%
  • the phase diagram further comprises a range (designated with G or L) where the fractions of the gas mixture form one phase (the mixing range) and a more or less closed range (designated with G+L, L+S and G+L+S) where at least a part of the fractions form a distinct phase (demixing range).
  • G the gas mixture is gaseous
  • L the gas mixture is liquid
  • G+L a mixture is present of liquid and gas, wherein in the present case HCN is in the liquid phase and CO 2 in the gaseous phase.
  • Present in range G+S+L is a mixture of gas, liquid and solid.
  • a number of lines demarcate the relevant ranges, in particular a dew point line 110 which indicates the boundary between combinations of pressure 100 and temperature 200 below which (in addition to other phases) a liquid phase L also occurs, and a solid line 120 which indicates the boundary between combinations of pressure 100 and temperature 200 below which (in addition to other phases) a solid phase S also occurs.
  • the phase diagram shows a critical point 140, a concept generally known to the skilled person, at which the gaseous phase and liquid phase are in equilibrium with each other.
  • the critical temperature is indicated in the phase diagram of figure 3 with T cnt .
  • a device 1 for cleaning a contaminated gas such as for instance the above stated CCVcontaining flue gas, in which device 1 the method according to the invention can be performed.
  • the contaminated gas is supplied as according to arrow Pi by a feed 2 under a pressure of between 100 and 300 Bar (usually a typical pressure of about 250 Bar) and at a temperature of for instance more than 100 0 C.
  • the gas supplied as according to arrow Pi is optionally cooled in a heat exchanger 3, for instance by means of cooling into the atmosphere. The cooling is such that the gas mixture is brought to a temperature which keeps the mixture gaseous.
  • the gas is preferably cooled at almost constant pressure.
  • the thus obtained gas mixture flows from heat exchanger 3 as according to arrow P 2 to a throttle valve 4.
  • the gas mixture supplied as according to arrow P 2 is expanded by means of throttle valve 4, preferably in isentropic manner, to a lower pressure of between for instance 5 and 20 Bar.
  • This isentropic pressure and temperature decrease is indicated in figures 2 and 3 by means of line 130.
  • T e final temperature
  • p e final pressure
  • the CO 2 fraction will become liquid.
  • the HCN fraction will become liquid.
  • the final temperature T e is preferably relatively close to, for instance a maximum of 50 0 C higher than, the temperature which corresponds at the final pressure p e with the transition of at least one of the fractions of the gas mixture to the solid phase which, referring to figures 2 and 3, is the temperature Ts.
  • the CO 2 fraction will become solid at T s , for the 50/50 mol% HCN/CO 2 mixture the HCN fraction.
  • This gas/liquid droplet mixture 5 is carried through channels 6 of a rotor 7 whereby, as a result of the rotation R of rotor 7, the CO 2 or HCN liquid droplets condense against the sides of channels 6 of rotor 7 which are directed toward a rotation shaft 8.
  • the condensed liquid droplets are collected in a basin 10 which can be emptied by means of activating a pump 11 such that the liquid fraction is discharged as according to arrow P 3 .
  • This discharge must preferably take place in cooled manner, at least for CO 2 , in order to keep the CO 2 liquid.
  • the gaseous phase leaves rotor 7 on the side remote from throttle valve 4 as a gas flow 12.
  • the gas flow 12 with the CO 2 at least largely removed and containing substantially H 2 is extracted and leaves device I as according to arrow P 4 as cleaned gas.
  • the gas flow substantially comprises CO 2 , with HCN at least partly removed.
  • the gas/liquid droplet mixture 5 created by the method according to the invention can be separated beforehand by being subjected to gravitational force.
  • the gas it is also possible according to a second preferred embodiment of the method according to the invention for the gas to be cooled at almost constant pressure to temperature T e , as indicated by line 140.
  • the gas it is also possible for the gas to be cooled to final temperature T 6 by means of a Joule Thompson condenser, as indicated by line 150.
  • a 50/40/10 mol% gas mixture of respectively H 2 , CO 2 and N 2 was separated into a gas flow and a liquid flow at a final temperature T e of -55°C and a final pressure P e of 45 Bar.
  • the gas flow contained 66.6 mol% H 2 , 20.3 mol% CO 2 and 13.1 mol% N 2 .
  • the liquid flow contained 0.5 mol% H 2 , 98.9 mol% CO 2 and 0.6 mol% N 2 .
  • the molar fraction of gas/liquid amounted to about 0.75/0.25. An almost purely CO 2 liquid flow is therefore obtained with the method.
  • the residue gas flow contains only about 20 mol% CO 2 .
  • the total quantity of CO 2 recovered from the original gas mixture amounts to about 62%.
  • the above obtained gas flow was then fed once again to the device shown in figure 1 and subjected for a second time to the method according to the invention.
  • the gas flow contained 66.6 mol% H 2 , 20.3 mol% CO 2 and 13,1 mol% N 2 , and after the separation 70.2 mol% H 2 , 16.1 mol% CO 2 and 13.7 mol% N 2 .
  • the liquid flow contained 0.9 mol% H 2 , 98.2 mol% CO 2 and 0.9 mol% N 2 .
  • the molar fraction of gas/liquid amounted this time to about 0.95/0.05.
  • the quantity of CO 2 recovered from the original gas mixture in the second step amounts to about 25%.
  • the total quantity of CO 2 recovered from the original gas mixture thus amounts to about 75% for the two steps together. This is higher than has heretofore been usual, certainly taking into account the limited amount of steps (two).
  • a 50/50 mol% gas mixture of respectively HCN and CO 2 was separated into a gas flow and a liquid flow at a final temperature T e of 25 0 C and a final pressure p e of 10 Bar.
  • the CO 2 is in the gaseous phase, while the HCN is substantially in the liquid phase.
  • the gas flow contained 89.7 mol% CO 2 and 10.3 mol% HCN.
  • the liquid flow contained 91.0 mol% HCN and 8.9 mol% CO 2 .
  • the molar fraction of gas/liquid amounted to about 0.51/0.49. It is thus possible with the invented method to separate a large part of the HCN and the CO 2 in a single process step, wherein each fraction has about 90 mol% purity.

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Abstract

L'invention porte sur un procédé pour séparer le CO2 d'un mélange de gaz de combustion ou de gaz de synthèse provenant de procédés de conversion de combustibles fossiles et de biocombustibles. Le procédé comprend les étapes de traitement consistant à utiliser un mélange gazeux contenant du CO2 à une pression de départ et à une température de départ, refroidir le mélange gazeux à une température finale et à une pression finale auxquelles au moins l'une des fractions présentes se trouve au moins partiellement dans la phase liquide du mélange gazeux, soumettre le mélange de milieu ainsi obtenu à une force volumique et évacuer au moins le CO2 sous forme de l'une des fractions séparées. L'invention porte également sur un dispositif pour séparer le CO2 du mélange gazeux.
PCT/NL2008/050323 2007-05-29 2008-05-28 Procédé et dispositif pour séparer le co2 d'un mélange de gaz de combustion ou de gaz de synthèse provenant de procédés de conversion de combustibles fossiles et de biocombustibles WO2008153379A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL2000665 2007-05-29
NL2000665A NL2000665C2 (nl) 2007-05-29 2007-05-29 Werkwijze en inrichting voor het separeren van CO2 uit een rook-of synthesegasmengsel van fossiel en biomassa gestookte processen.

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010130781A1 (fr) 2009-05-15 2010-11-18 Shell Internationale Research Maatschappij B.V. Procede et systeme de separation de co2 d'un gaz de synthese ou d'un gaz de carneau
WO2011054803A1 (fr) 2009-11-03 2011-05-12 Shell Internationale Research Maatschappij B.V. Separation centrifuge de co2 condense a partir d'un gaz combustion
IT201600081328A1 (it) * 2016-08-02 2018-02-02 Saipem Spa Recupero di anidride carbonica da gas di sintesi in impianti per la produzione di ammoniaca per mezzo di separazione gravimetrica

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IT201600081328A1 (it) * 2016-08-02 2018-02-02 Saipem Spa Recupero di anidride carbonica da gas di sintesi in impianti per la produzione di ammoniaca per mezzo di separazione gravimetrica
WO2018025197A1 (fr) * 2016-08-02 2018-02-08 Saipem S.P.A. Récupération de dioxyde de carbone à partir de gaz de synthèse dans des installations pour la production d'ammoniac par séparation gravimétrique

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