WO2014194376A1 - Benzylamine, dérivés de benzylamine et mélanges de benzylamines pour l'élimination de co2 de flux gazeux - Google Patents

Benzylamine, dérivés de benzylamine et mélanges de benzylamines pour l'élimination de co2 de flux gazeux Download PDF

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WO2014194376A1
WO2014194376A1 PCT/AU2014/000859 AU2014000859W WO2014194376A1 WO 2014194376 A1 WO2014194376 A1 WO 2014194376A1 AU 2014000859 W AU2014000859 W AU 2014000859W WO 2014194376 A1 WO2014194376 A1 WO 2014194376A1
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substituted
alkyl
unsubstituted
solution
group
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PCT/AU2014/000859
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English (en)
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Graeme PUXTY
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Commonwealth Scientific And Industrial Research Organisation
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Priority claimed from AU2013903284A external-priority patent/AU2013903284A0/en
Application filed by Commonwealth Scientific And Industrial Research Organisation filed Critical Commonwealth Scientific And Industrial Research Organisation
Publication of WO2014194376A1 publication Critical patent/WO2014194376A1/fr
Priority to AU2015218491A priority Critical patent/AU2015218491A1/en
Priority to US14/838,608 priority patent/US20150367281A1/en
Priority to CN201510549197.9A priority patent/CN105381686A/zh

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    • 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
    • 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
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0233—Other waste gases from cement factories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/025—Other waste gases from metallurgy plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • 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 present invention is directed to an absorbent solution for absorbing an acidic gas, such as carbon dioxide, from a gas stream.
  • an acidic gas such as carbon dioxide
  • Waste gas emissions are of significant concern, and the presence of certain gaseous constituents in a waste gas stream can result in air pollution.
  • Carbon dioxide (C0 2 ) emissions in particular, attract a great deal of attention and the discussion of waste gas emissions that follows will largely be in respect of carbon dioxide. However, the skilled addressee will appreciate that much of this discussion is also applicable to other waste gases.
  • CO 2 carbon dioxide
  • post combustion capture The process for capturing CO 2 from power station or combustion device flue gases is termed post combustion capture.
  • post combustion capture the CO 2 in flue gas is first separated from nitrogen and residual oxygen using a suitable solvent in an absorber.
  • the CO 2 is then removed from the solvent in a process called stripping (or regeneration), thus allowing the solvent to be reused.
  • stripping or regeneration
  • the stripped CO2 is then liquefied by compression and cooling, with appropriate drying steps to prevent hydrate formation.
  • Post combustion capture in this form is applicable to a variety of stationary CO 2 sources including power stations, steel plants, cement kilns, calciners and smelters.
  • the capture process involves a series of chemical reactions that take place between water, the amine and carbon dioxide.
  • Amines are weak bases, and may undergo acid-base reactions.
  • the aqueous CO 2 reacts with water and the neutral form of the amine react to generate carbonic acid (H 2 CO 3 ), aqueous bicarbonate (HCO 3 " ) ions and aqueous carbonate (CO 3 2" ) ions, according to the generally acknowledged equations described below:
  • the carbamate may also then participate in acid-base chemistry, according to the generally acknowledged reactions described below.
  • Tertiary amines R a R b R c N, R a , R b R c ⁇ H) cannot form carbamates.
  • Carbamate formation by primary and secondary amines is a direct reaction between the amine nitrogen and CO2. This reaction consumes two moles of amine per mole of C0 2 absorbed. One mole is amine that is converted to carbamate, and the second is amine that accepts the proton released by carbamate formation. Carbamate is also a base, as illustrated by the reaction of equation 8 to form carbamic acid. However, it is a much weaker base than an amine and as such does not contribute as a proton acceptor at typical CO 2 absorption conditions. The stability of the carbamate species is influenced only weakly by temperature (the reaction enthalpy is small).
  • CO2 desorption is achieved by heating of an aqueous amine solution containing CO 2 .
  • the two major effects of heating are to reduce the physical solubility of CO2 in the solution, and to reduce the pK a of the amine resulting in a concomitant reduction in pH and in CO2 absorption capacity, the net effect of which is CO2 release.
  • the extent of the reduction in pK a is governed by the enthalpy of the amine protonation reaction which in turn is governed by the amine chemical structure. All the other reactions, including carbamate formation, have small reaction enthalpies and are insensitive to temperature.
  • the enthalpy of amine protonation is four to eight times larger than the enthalpies of the carbonate reactions and two to four times larger than the enthalpy of carbamate formation. It is the lowering of the pH upon heating that drives the reversal of carbamate and carbonate/bicarbonate formation during desorption, rather than any significant reduction in stability.
  • Amines such as MEA also suffer from oxidative and thermal degradation due to exposure to molecular oxygen in flue gas, and heating to release absorbed CO2. This degradation requires ongoing reclamation and replenishment of the absorbent solution at considerable cost.
  • Amines such as MEA are also limited in the maximum concentration that can be used due to corrosion and viscosity.
  • MEA is limited to 30 wt% as at higher concentrations it becomes too corrosive for use in contact with carbon steel.
  • a process for absorbing target acidic gas from a gas stream rich in the target acidic gas comprising contacting the gas stream with a solution to absorb a target gas from a gas stream, the solution comprising a solvent and at least one absorbent compound dissolved in the solvent, said at least one absorbent compound comprising the compound of formula (1 ):
  • R 6 and R 7 are each independently selected from the group consisting of: H, substituted or unsubstituted Ci to C 2 o alkyl, substituted or unsubstituted C 2 to C 2 o alkenyl, and substituted or unsubstituted C 2 to C 2 o alkynyl; wherein R 8 and R 9 are independently selected from the group consisting of H, substituted or unsubstituted Ci to C 20 alkyl, substituted or unsubstituted C 2 to C 20 alkenyl, and substituted or unsubstituted C 2 to C 2 o alkynyl substituted or unsubstituted aryl, substituted or unsubstituted heterocycle, substituted or unsubstituted carbonyl, aldehyde, substituted or unsubstituted carboxylate, substituted or unsubstituted ester, substituted or unsubstituted alkoxy, substituted or unsubstituted carboxamide, substituted
  • no more than one of R 1 to R 5 is an alkyl amine. In one embodiment, none of R 1 to R 5 are alkyl amine. Preferably, none of R 1 to R 5 is an alkyl aryl. Preferably, no more than three, more preferably not more than two and even more preferably no more than one of R 1 to R 5 comprises a substituted or unsubstituted Ci to C 2 o alkyl. In another embodiment, no more than three, more preferably not more than two and even more preferably no more than one of R 1 to R 5 comprises a substituted or unsubstituted Ci to C 5 alkyl. Examples of substituted Ci to C 5 allyl include substitution with a substituent selected from the group consisting of hydroxyl, thiol, amino, alkoxy and carboxyl.
  • the group substituted or unsubstituted carbonyl may be acyl such as a hydrocarbyl-carbonyl where the hydrocarbyl may be selected from group consisting of aryl, Ci to C 20 alkyl, C 2 to C 20 alkenyl and C 2 to C 20 alkynyl.
  • the group substituted or unsubstituted carboxyl may be carboxyl or hydrocarbyloxycarbonyl wherein the hydrocarbyl is selected from the group consisting of aryl, Ci to C 20 alkyl, C 2 to C 2 o alkenyl and C 2 to C 2 o alkynyl.
  • the group substituted or unsubstituted ester may be an acyloxy wherein the group acyl is hydrocarbyl-carbonyl where the hydrocarbyl may be selected from group consisting of aryl, Ci to C 2 o alkyl, C 2 to C 2 o alkenyl and C 2 to C 2 o alkynyl.
  • R 1 and R 5 are selected to enhance the solubility of the absorbent in the solvent.
  • R 1 to R 5 are at least one (preferably at least 2 and more preferably at least 3) of R 1 to R 5 are selected from substituents which are capable of hydrogen bonding with the aqueous solvent.
  • substituents capable of forming hydrogen bonding with aqueous solvents may be selected from the group consisting of hydroxyl, hydroxyalkyi, alkoxy, thiol, amino (i.e. -NH 2 ) carboxyl and aryloxy.
  • R 1 to R 5 are selected from the group consisting of H, hydroxyl, hydroxyalkyi, alkoxy, thiol or amino.
  • the one of the substituents R 1 to R 5 is Ci to C 6 alkyl and the remaining substituents are selected from the group consisting of H, hydroxyl, hydroxyl-Ci to C5 alkyl, alkoxy, thiol and amino.
  • R 1 to R 5 are H or one of R 1 to R 5 is Ci to C 4 alkyl (such as methyl) and the others are H.
  • the nitrogen substituents R 6 and R 7 are each hydrogen (H). Compounds wherein R 6 and R 7 are both hydrogen generally exhibit improved solubility in the relevant solvents such as water and protic and/or a polar aprotic solvents.
  • absorbent compounds of formula (1 ) have lower susceptibility to thermal and oxidative degradation than a 30 wt% MEA solution due to the inherent chemical stability imparted by the aromatic ring structure.
  • the cyclic absorption capacity of the solution for the target gas is comparable to that of a tertiary or sterically hindered amine solution and the rate of absorption of the target gas is comparable to or better than a 30wt% MEA solution.
  • the solution is preferably a single phase liquid solution prior to the absorption of the acid gas as well as after the absorption of the acid gas (i.e. no precipitation of the reactants of the absorption process).
  • the absorbent may be dissolved or disperse in one or more solvents.
  • the solvent is typically an organic solvent, water or a combination thereof.
  • the organic solvents are preferably a protic and/or a polar aprotic solvent. Suitable solvents that may be used include, but are not limited to, methanol, ethanol, propenol, glycols, carbonates (e.g.
  • the target gas is an acidic gas.
  • the target gas is selected from the group consisting of CO 2 , NO x (where x is between 0.5 and 2), SO 2 , H 2 S, carbonyl sulphide, carbon disulfide, thiols or a halogen gas, such as Cl 2 , F 2 , l 2 , or Br 2 . More preferably the target gas is C0 2 or S0 2 . Most preferably the target gas is C0 2 .
  • a number of target gases may be absorbed from a gas stream using the solution of the present invention, the target gases being selected from various combinations of C0 2 , NO x , S0 2 , H 2 S or a halogen gas, such as Cl 2 , F 2 , l 2 , or Br 2 .
  • the target gas is C0 2 .
  • the solution is an aqueous solution.
  • the solvent may also be any protic solvent such as methanol, n-butanol or glycol or polar aprotic solvent such as ethylacetate or dimethylsulfoxide in which the acid gas and amine are jointly soluble.
  • the target gas to be absorbed from the gas stream needs to be at least partially soluble in the solvent, so that the target gas is able to interact with the various constituents of the solution.
  • the solvent comprises a mixture of water and a protic solvent (e.g.
  • a co-solvent to replace part of the water as a solvent may be influenced by improved characteristics of the co-solvent, resulting in a solvent mixture with increased acidic gas solubility, lower heat capacity or a higher boiling point.
  • R 1 to R 5 are each independently selected from the group consisting of: H, hydroxyl, or Ci to C 10 alkyl; R 6 and R 7 are independently selected from the group consisting of H, methyl, or ethyl. More preferably the absorbent compound is benzylamine or a benzylamine derivative. Most preferably the compound is benzylamine.
  • the compound of formula (1 ) is present in the solution in an amount of at least 1 % (such as 1 % to 70 %) by weight based on the weight of the solution.
  • the compound of formula 1 is preferably present in an amount between 1wt % and 50wt%, more preferably 1 .5wt% and 40wt%, even more preferably between 2wt% and 30wt% and even more preferably between 5wt% and 20wt% based on the total weight of the solution.
  • the upper limit of the compound of formula (1 ) is limited by the concentration which results in the precipitation of the reactants of the absorbent(s) and the absorbed acid gases.
  • the upper limit of the compound of formula (1 ) is preferably 70wt%, more preferably 65wt%, even more preferably 60wt% and yet even more preferably 55wt% of the total weight of the solution.
  • the total concentration of acidic gas absorbant compounds including the compounds of formula (1 ) is preferably at least about 10 weight %. More preferably the concentration is at least about 20 weight %. Even more preferably the concentration is at least about 30 weight %. Yet even more preferably the concentration is at least about 40 weight %. Most preferably the concentration is at least about 50 weight % or above 50 weight %.
  • the solution has a low viscosity and low corrosion potential.
  • This allows the solution to contain the compounds at high concentration while still being able to maintain effective operating conditions.
  • This provides for a solution with a large target gas absorption capacity and target gas absorption rate.
  • the viscosity of the solution measured at 40°C is less than 3mPa.s. More preferably, the viscosity of the solution is less than 2.75mPa.s. Even more preferably, the viscosity is less than 2.5mPa.s.
  • the at least one absorbent compound dissolved in the solvent will comprise the compound of formula (1 ) which may constitute the total of the gas absorbent compound or may be present in solution with other acidic gas absorbent compounds so that the total gas absorbent compounds comprise one or more gas absorbent compounds in addition to the compounds of formula (1 ).
  • the solution contacted with the gas stream comprises one or more acidic gas absorbing compounds selected from amines and imidazoles in addition to the compound of formula (1 ).
  • the one or more additional amines may be selected from primary, secondary and tertiary amines.
  • Suitable amines include primary amines such as monoethanolamine, ethylenediamine, 2-amino-2-methylpropanol, 2-amino-2-methyl- ethanolamine and benzylamine; secondary amines such as N-methylethanolamine, piperazine, piperidine and substituted piperidine, diethanolamine, diglycolamine and diisopropanolamine; and tertiary amines such as N-methyldiethanolamine, and amino acids such as taurine, sarcosine and alanine.
  • primary amines such as monoethanolamine, ethylenediamine, 2-amino-2-methylpropanol, 2-amino-2-methyl- ethanolamine and benzylamine
  • secondary amines such as N-methylethanolamine, piperazine, piperidine and substituted piperidine, diethanolamine, diglycolamine and diisopropanolamine
  • tertiary amines such as N-methyldiethanolamine, and amino acids such as taurine
  • the solution further includes an additional amine compound, such as a tertiary or sterically hindered amine.
  • the additional amine compound helps to avoid precipitation of the absorbent compound out of solution, which may be an issue at high weight loadings of the absorbent compound, and/or depending on the chemical environment of the solution.
  • Suitable compounds may include for example: 2-amino-2-methyl-1 -propanol (AMP), 3-piperidinemethanol, 3-piperidineethanol, 2- piperidinemethanol, 2-piperidineethanol, N-piperidinemethanol, N-piperidineethanol, 2-methylaminoethanol, ⁇ , ⁇ -dimethylaminoethanol and 3-quinclidinol.
  • the compound is not monoethanolamine, diethanolamine, aminoethylethanolamine, Diglycolamine, piperazine, N- Aminoethylpiperazine, N-(2-hydroxyethyl) piperazine and morpholine
  • the solution comprises an imidazole and more preferably an N-functionalised imidazole.
  • Suitable N-functionalised imidazoles may be found in US8741246, which in incorporated herein by reference.
  • R 1 is substituted or unsubstituted Ci -2 o alkyl, substituted or unsubstituted C 2-20 alkenyl, substituted or unsubstituted C 2-2 o alkynyl, substituted or unsubstituted Ci -2 o heteroalkyl, substituted or unsubstituted C 2-2 o heteroalkeroalkyl, substituted or unsubstituted C 2-20 heteroalkenyl, substituted or unsubstituted C 2-20 heteroalkynyl, substituted or unsubstituted cycloalkyl, substituted or unsubstituted heterocycloalkyi, substituted or unsubstituted aryl, substituted or unsubstituted heteroaryl, substituted or unsubstituted thio, substituted or unsubstituted amino, substituted or unsubstituted alkoxyl, substituted or unsubstituted aryloxyl, silyl, siloxy
  • R 2 , R 3 , and R 4 are each independently selected from hydrogen, halogen, hydroxyl, substituted or unsubstituted Ci -2 o alkyl, substituted or unsubstituted C 2-2 o alkenyl, substituted or unsubstituted C 2-2 o alkynyl, substituted or unsubstituted Ci -2 o heteroalkyl, substituted or unsubstituted C 2-20 heteroalkenyl, substituted or unsubstituted C 2-20 heteroalkynyl, substituted or unsubstituted cycloalkyl, substituted or unsubstituted heterocycloalkyi, substituted or unsubstituted aryl, substituted or unsubstituted heteroaryl, substituted or unsubstituted thio, substituted or unsubstituted alkoxyl, aryloxyl, substituted or unsubstituted amino, cyano, or nitro.
  • the solution comprises a combination of N-functionalised imidazoles and one or more amines.
  • the one or more amines which may be used in addition to the N-functionalised imidazoles may be selected from the group consisting of primary, secondary and tertiary amines including the specific examples of such amines referred to above.
  • the total wt% of the at least one absorbent compound in solution is preferably at least 20wt%, more preferably at least 25 wt %, still more preferably at least 30wt%, even more preferably at least 40wt% and yet even more preferably at least 50wt% relative to the total weight of the solution.
  • This component will typically consists of the compound of formula (1 ) and optionally one or more compounds selected from amines and N-functionalised-imidazoles.
  • the compound of chemical formula (1 ) preferably comprises at least 1 % (e.g.
  • 1 % to 70% more preferably between 1wt% and 50wt%, still more preferably between 1.5wt% and 40wt%, even more preferably between 2 wt% and 30wt% and even more preferably between 5wt% and 20wt% relative to the total weight of the solution.
  • a process for removing a target gas from a gas mixture including: contacting a gas mixture that is rich in target gas with an absorbent solution, as described above, to form a target gas rich solution and a gas mixture that is lean in target gas; and desorbing the target gas from the target gas rich solution.
  • composition comprising a solution for an acidic gas comprising:
  • R 6 and R 7 are each independently selected from the group consisting of: H, substituted or unsubstituted Ci to C 20 alkyi, substituted or unsubstituted C 2 to C 20 alkenyl, and substituted or unsubstituted C 2 to C 2 o alkynyl (more preferably R 6 and R 7 are both hydrogen); wherein R 8 and R 9 are independently selected from the group consisting of H, substituted or unsubstituted Ci to C 20 alkyi, substituted or unsubstituted C 2 to C 20 alkenyl, and substituted or unsubstituted C 2 to C 20 alkynyl substituted or unsubstituted aryl, substituted or unsubstituted heterocycle, substituted or unsubstituted carbonyl, substituted or unsubstituted aldehyde, substituted or unsubstituted carboxylate, substituted or unsubstituted ester, substituted or unsubstituted alkoxy,
  • an absorbed acidic gas preferably carbon dioxide, at a concentration above the equilibrium concentration when the solution is exposed to air at below the boiling point of the solvent.
  • the concentration of the absorbed acidic gas is more than two times (and even more preferably five times) the equilibrium concentration when the solution is exposed to air at belo the boiling point of the solvent, thus representing the absorbed acidic gas concentration in the solvent during the absorption process as previously described.
  • the background amount of acidic gas such as CO2
  • the absorbed acidic gas will constitute at least 0.2% by weight based on the total weight of the solution on absorption of the gas more preferably at least 1 % and still more preferably at least 10% absorbed acidic gas by weight based on the total weight of the solution.
  • the solution comprises one or more amines in addition to the compound of formula (1 ⁇ which additional amines may, for example, be selected from primary, secondary and tertiary amines optionally including N-functionalised imidazoles such as those of formula (2).
  • Figure 1 illustrates a process for removing a target gas from a gas mixture according to the present invention.
  • Figure 2 is a graph showing CO2 loading per kg of absorbent solution at different C0 2 partial pressures for a range of different solutions.
  • Figure 3 is a graph showing the evolution of the CO 2 partial pressure with time.
  • Figure 4 is a graph showing the viscosity of absorbent solutions containing varying amounts of benzylamine or MEA at different temperatures.
  • Figure 5 is a graph showing the overall mass transfer coefficient for various CO 2 loadings/mole amine for a range of amines including mixtures of benzylamine and 2-amino-2-methyl-1 -propanol (AMP) compared with MEA.
  • Figure 6 is a graph showing the overall mass transfer coefficient for various C0 2 loadings/mole amine for mixtures of benzylamine and MEA compared with MEA above.
  • the invention relates to the use of a solution including benzylamine, a benzylamine derivative, a benzylamine mixture, a benzylamine derivative mixture, or a combination thereof in a solution for absorbing a target gas from a gas stream.
  • Figure 1 provides an illustration of an embodiment of a process for capture of a target gas from a flue gas stream.
  • the target gas is C0 2 .
  • the process 100 includes an absorption reactor 102, for absorbing C0 2 from a flue gas stream, and a desorption reactor 104 for desorbing CO 2 .
  • the absorption reactor 102 includes a first inlet 106, a second inlet 108, a first outlet 110, and a second outlet 1 12, and a gas absorption contact region 114.
  • the first inlet 106 of the absorption reactor 102 is a flue gas inlet through which a C0 2 rich flue gas enters the absorption column 102.
  • the second inlet 108 is an absorbent solution inlet through which a CO 2 lean absorbent enters the absorption column 102.
  • the CO 2 rich flue gas and the CO 2 lean absorbent contact in the gas absorption contact region 114. In this region the C0 2 in the C0 2 rich flue gas is absorbed into the absorbent solution where it is bound in solution to form a C0 2 lean flue gas and a CO 2 rich absorbent solution.
  • the absorbent solution includes an absorbent molecule.
  • the absorbent molecule is benzylamine, e.g.:
  • the local environment of the soiution may be altered in the absorption column to favour the absorption reaction, e.g. to increase absorption of COa into solution where it is bound to the benzylamine.
  • Such alterations of the local environment may include a change in pH, a change in solution temperature, a change in pressure etc.
  • the soiution may include other compounds which assist in the absorption of COa. These compounds may alter the affinity or absorption capacity of the benzylamine for CO2, or these compounds may be also absorb CO2.
  • the process may additionally include means to remove these compounds.
  • the absorption of CO 2 from the CO2 rich f!ue gas into the absorbent solution results in a C0 2 lean gas and a CO 2 rich absorbent soiution.
  • the CO 2 lean gas may still include some C0 2 , but at a lower concentration than the C0 2 rich flue gas, for example a residual concentration of C0 2 .
  • the CO 2 lean gas leaves the absorption column 102 through the first outlet 110, which is a C0 2 lean gas outlet.
  • the C0 2 rich absorbent solution leaves the absorption column through the second outlet 1 12, which is a CO2 rich absorbent outlet.
  • Desorption reactor 104 includes an inlet 1 18, a first outlet 120, a second outlet 122, and a gas desorption region 124.
  • the C0 2 rich absorbent outlet 1 12 of the absorption column 102 forms the inlet 1 18 of the desorption column 104. Desorption of C0 2 from the C0 2 rich solution occurs in the gas desorption region 124.
  • Desorption of C0 2 from the C0 2 rich solution may involve the application of heat or a reduction in pressure to favour the desorption process.
  • additional compounds may be added to the C0 2 rich solution to enhance the desorption process.
  • Such compounds may alter the solution environment, for example by changing solution pH or altering another parameter to favour the desorption reaction.
  • C0 2 lean absorbent solution may still include some C0 2 , but at a lower concentration than the C0 2 rich solution, for example a residual concentration of C0 2 .
  • the C0 2 gas stream is taken off via the first outlet 120, which is a C0 2 outlet.
  • the C0 2 lean absorbent solution is taken off via the second outlet 122, which is a C0 2 lean absorbent solution outlet.
  • the C0 2 lean absorbent is then recycled and fed through the second inlet 108 to the absorption column 102.
  • the amount of solvent circulating in a PCC process is linearly related to cyclic CO 2 mass absorption capacity of the solvent between the absorption (rich) and desorption (iean) column temperatures.
  • Concentrated benzylamine solvents show superior absorption capacity compared to MEA 30 wt%, but the concentration of BA is limited by precipitation.
  • the optimal concentration of BA is at the limit of precipitation when at equilibrium with 15 kPa COs.
  • the cyclic capacity is estimated to be 0.04 kg C0 2 /kg solvent, compared with 0.021 kg CO2/ kg solvent for MEA 30 wt%.
  • Precipitation can be avoided by the use of a second amine such as AMP.
  • the enhancement factor, E, in amine mixture was determined by C0 2 initial rate absorption at 40°C in a pressurised stirred-vessei with a flat gas-liquid interface with MDEA-BA and compared to MEA- DEA and DEA-MDEA.
  • the initial partial pressure in the vessel was about 5 bar C0 2 .
  • the evolution of the C0 2 partial pressure with time is shown in Figure 3.
  • Benzylamine performed as well as or better than MEA and DEA as a rate promoting agent.
  • a larger amount of benzylamine in aqueous MDEA resulted in a higher enhancement of the C0 2 absorption rate. Due to the favourable physical properties of benzylamine use at higher concentrations is possible.
  • Viscosities, ⁇ in Pa.s, of concentrated benzylamine aqueous solutions were measured between 25°C and 80°C with an Anton Paar AMVn viscometer. Corresponding densities are required for the determination of ⁇ and were measured with a benchtop density meter (Anton Paar DMA 38).
  • the maximum viscosity (2.51 mPa.s) was measured with BA 75wt%. This value is reasonably low compared to that of MEA 80wt% (10.2 mPa.s) as depicted in Figure 4. Therefore, viscosity of concentrated benzylamine aqueous solutions would not raise operability issues such as solvent's pumpability and pourability.
  • low viscosity is also favourable for the diffusion rate of a C0 2 in the solvent as the diffusion rate is inversely proportional to the liquid viscosity (Stokes-Einstein equation).

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  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
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Abstract

L'invention concerne un procédé d'élimination d'un gaz acide cible d'un flux gazeux riche en gaz acide cible consistant à mettre en contact le flux gazeux avec une solution pour absorber un gaz cible d'un flux gazeux, la solution comprenant un solvant et au moins un composé absorbant dissout dans l'eau, ledit au moins un composé absorbant comprenant un composé représenté par la formule (1).
PCT/AU2014/000859 2013-08-29 2014-08-29 Benzylamine, dérivés de benzylamine et mélanges de benzylamines pour l'élimination de co2 de flux gazeux WO2014194376A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
AU2015218491A AU2015218491A1 (en) 2014-08-29 2015-08-27 Absorbent solution for absorption of acid gas and process for absorption of acid gas
US14/838,608 US20150367281A1 (en) 2013-08-29 2015-08-28 Absorbent solution for absorption of acid gas and process for absorption of acid gas
CN201510549197.9A CN105381686A (zh) 2014-08-29 2015-08-31 用于吸收酸气体的吸收剂溶液和用于吸收酸气体的方法

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
AU2013903284A AU2013903284A0 (en) 2013-08-29 Benzylamine, benzylamine derivatives and benzylamine mixtures for Co2 removal from gas streams
AU2013903284 2013-08-29
AU2014901053A AU2014901053A0 (en) 2014-03-25 Benzylamine, benzylamine derivatives and benzylamine mixtures for co2 removal from gas streams
AU2014901053 2014-03-25

Related Child Applications (1)

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CN104645780A (zh) * 2015-02-04 2015-05-27 中国华能集团清洁能源技术研究院有限公司 一种捕集二氧化碳的变温浓缩吸收剂及其使用方法
WO2016116815A1 (fr) * 2015-01-22 2016-07-28 Carbon Clean Solutions Limited Solvant et procédé permettant d'éliminer des gaz acides d'un mélange gazeux
WO2020220064A1 (fr) * 2019-05-02 2020-11-05 Commonwealth Scientific And Industrial Research Organisation Processus de régénération d'un absorbant liquide
WO2022257197A1 (fr) * 2021-06-09 2022-12-15 华东理工大学 Application d'un composé amine dans l'élimination de sulfures organiques

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2016116815A1 (fr) * 2015-01-22 2016-07-28 Carbon Clean Solutions Limited Solvant et procédé permettant d'éliminer des gaz acides d'un mélange gazeux
CN104645780A (zh) * 2015-02-04 2015-05-27 中国华能集团清洁能源技术研究院有限公司 一种捕集二氧化碳的变温浓缩吸收剂及其使用方法
CN104645780B (zh) * 2015-02-04 2016-06-08 中国华能集团清洁能源技术研究院有限公司 一种捕集二氧化碳的变温浓缩吸收剂及其使用方法
WO2020220064A1 (fr) * 2019-05-02 2020-11-05 Commonwealth Scientific And Industrial Research Organisation Processus de régénération d'un absorbant liquide
US11607642B2 (en) 2019-05-02 2023-03-21 Commonwealth Scientific And Industrial Research Organisation Process for regenerating a liquid absorbent
WO2022257197A1 (fr) * 2021-06-09 2022-12-15 华东理工大学 Application d'un composé amine dans l'élimination de sulfures organiques

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