• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A process for removing acid gases from a water vapour-containing fluid stream (1) comprises a) providing an absorption liquid (16) which is incompletely miscible with water; b) treating the fluid stream (1) in an absorption zone (3) with the absorption liquid (16) to obtain an acid gas-depleted treated fluid stream (4) and an acid gas-loaded absorption liquid (7); c) directing the treated fluid stream (4) to a rehydration zone (5) and treating the fluid stream (4) with an aqueous liquid (22) to volatilize at least part of the aqueous liquid; d) regenerating (12) the loaded absorption liquid (9, 11) to expel the acid gases (17) at least in part and obtain a regenerated absorption liquid (13), and directing the regenerated absorption liquid (13, 14, 16) to step b); and e) separating (8), from the absorption liquid (7), an aqueous liquid (22) that has condensed in the absorption zone (3), and directing the aqueous liquid (22) to step c). The process allows for an efficient removal of water accumulated in the absorption liquid system.
    公开号:AU2013225124A1
    申请号:U2013225124
    申请日:2013-02-26
    公开日:2014-09-25
    发明作者:Torsten Katz；Christian Riemann；Georg Sieder
    申请人:BASF SE；
    IPC主号:B01D53-14
    专利说明:
    WO 2013/127765 PCT/EP2013/053775 1 Removing acid gases from water vapour-containing fluid streams The present invention relates to a process for removing acid gases from a water va pour-containing fluid stream, in particular for removing carbon dioxide from combustion 5 exhaust gases. Combustion of fossil fuels generates the acid gases, carbon dioxide (C0 2 ), sulfur ox ides (SO 2 ), carbonyl sulfide (COS), hydrogen sulfide (H 2 S) and nitrogen oxides (NOx). Emission of acid gases into the air is considered to be the main cause of global effects 10 on the environment which are termed the greenhouse effect. The removal of acid gas es from combustion exhaust gases is therefore desirable to reduce the environmental effects of these sources. Current aqueous scrubbing technologies remove acid gases by treating the fluid 15 streams with aqueous solutions of inorganic or organic bases, e.g. alkanolamines, as absorbents. On the dissolution of acid gases, ionic products form from the base and the acid gas components. The absorbent can be regenerated by heating, expansion to a lower pressure or stripping, in which case the ionic products react back to acid gases and/or the acid gases are stripped off by means of steam. After the regeneration pro 20 cess the absorption liquid can be reused. Non-aqueous absorption liquids have been used to remove acid gases from fluid streams. It is claimed that non-aqueous absorption liquids require less energy for re generation than aqueous solutions of organic bases. Single-component alcoholic phy 25 sisorption solvents such as RECTISOL@ and SELEXOL@ are commercially available for CO 2 separation but perform poorly in the humid, near-ambient pressure conditions associated with combustion exhaust gas. Ionic liquids are another non-aqueous absorption liquid currently being developed. 30 These absorption liquids have higher CO 2 loadings than some aqueous amines, and are regenerable under milder conditions. WO 2009/097317 discloses reversible acid-gas binding liquid systems that permit cap ture of acid gases and release of the acid gases from the liquid by the activation of a 35 trigger. The exemplified systems are equimolar mixtures of amidine or guanidine nitro gen bases and alcohols. They are non-ionic room temperature liquids that react with
    CO
    2 to form room-temperature ionic liquids. CO 2 is captured via the formation of amidinium and guanidinium alkyl carbonate salts derived from the conjugate bases of the deprotonated alcohol components.
    WO 2013/127765 PCT/EP2013/053775 2 Combustion exhaust gases typically contain appreciable amounts of water vapour or are water vapour-saturated. Upon contact of a non-aqueous absorption liquid with the water vapour-containing fluid stream, water vapour may condense and/or become dis 5 solved into the non-aqueous absorption liquid. On the other hand, the non-aqueous absorption liquid may not show a significant water vapour partial pressure, so that the treated fluid stream will not take up an appreciable amount of water vapour when leav ing the absorption unit. 10 These effects can lead to the accumulation of water in the absorption liquid either as a single-phase solution or bi-phase mixture, depending upon the process conditions (e.g., pressure, temperature, water concentration) and the affinity of the non-aqueous absorption liquid for water. Water accumulation is detrimental to the acid gas separa tion and purification process, since more energy will be required for absorption liquid 15 regeneration due to the necessity of continually removing water from the absorption liquid. Thus, the amount of water that accumulates in the absorption liquid system must be removed from the process in order to fulfil the overall water balance. 20 When the absorption liquid is incompletely miscible with water (or, in other words, shows a miscibility gap with water), the water introduced may sooner or later accumu late as a separate aqueous phase within the absorption liquid system. The aqueous phase may be separated by, e.g., a decanter, and discharged as a liquid bleed. Since, 25 however, the absorption liquid shows - even though limited - solubility in water the liq uid bleed contains traces of absorption liquid and will cause undesirable absorption liquid losses. To be properly discharged, the liquid bleed must be purified. Purification of the liquid bleed is costly and technically difficult and therefore not a preferred option. As a result, bleeding liquid water constitutes a clear economic and ecological disad 30 vantage and decreases the commercial attractiveness of the process. Accordingly, there is a need for a process for removing acid gases from a water va pour-containing fluid stream, which allows for an efficient removal of water accumulat ed in the absorption liquid system. 35 EP-A 2 228 119 discloses a method for removal of acid compounds from a gas by car rying out an absorption step with an absorption liquid. The treated gas is washed and cooled in a washing section by contacting with a liquid water flow having a predeter mined temperature, so as to obtain a washed gas whose temperature is lower than WO 2013/127765 PCT/EP2013/053775 3 temperature of the gas to be treated. A quantity of water contained in the acid com pound-rich effluent is withdrawn to prevent accumulation of water in the absorption liquid. 5 The invention provides a process for removing acid gases from a water vapour containing fluid stream comprising a) providing an absorption liquid which is incompletely miscible with water; b) treating the fluid stream in an absorption zone with the absorption liquid to obtain 10 an acid gas-depleted treated fluid stream and an acid gas-loaded absorption liq uid; c) directing the treated fluid stream to a rehydration zone and treating the fluid stream with an aqueous liquid to volatilize at least part of the aqueous liquid; d) regenerating the loaded absorption liquid to expel the acid gases at least in part 15 and obtain a regenerated absorption liquid, and directing the regenerated absorp tion liquid to step b); and e) separating, from the absorption liquid, an aqueous liquid that has condensed in the absorption zone, and directing the aqueous liquid to step c). 20 The absorption liquid used in the process is incompletely miscible with water or, in oth er words, shows a miscibility gap with water. In preferred embodiments, the absorption liquid is essentially immiscible with water. Generally, less than 20 % by weight of water is soluble in the absorption liquid at 25 'C, for example less than 10 % by weight or less than 8 % by weight, preferably less than 5 % by weight of water. If a higher 25 amount of water is present, a separate aqueous phase will form within the absorption liquid. The method according to the invention is suitable for the treatment of water vapour containing fluid streams, in particular water vapour-containing gas streams of all types. 30 The acid gases comprise, in particular, C0 2 , H 2 S, COS and mercaptans. In addition,
    SO
    3 , SO 2 , CS 2 and HCN can also be removed. Generally, the acid gases comprise at least CO 2 or may comprise exclusively CO 2 . The process according to the invention is particularly applicable to the treatment of fluid 35 streams wherein the partial pressure of acid gases in the fluid stream is less than 2 bar, preferably less than 1 bar, e.g. less than 500 mbar. Fluids, which comprise the acid gases are either gases such as natural gas, synthesis gas, coke oven gas, cracked gas, coal gasification gas, recirculated cycle gas, landfill WO 2013/127765 PCT/EP2013/053775 4 gases and combustion gases or liquids which are essentially immiscible with the ab sorbent such as liquefied petroleum gas (LPG) or natural gas liquids (NGL). In preferred embodiments, the fluid stream originates 5 i) from the oxidation of organic substances, ii) from the composting or storage of waste materials comprising organic substances, or iii) from the bacterial decomposition of organic substances. 10 The oxidation can be carried out with appearance of flame, i.e. as conventional com bustion, or as oxidation without appearance of flame, e.g. in the form of a catalytic oxi dation or partial oxidation. Organic substances which are subjected to the combustion are customarily fossil fuels, such as coal, natural gas, petroleum, gasoline, diesel, raffi 15 nates or kerosene, biodiesel or waste materials having a content of organic substanc es. Feed stocks of the catalytic (partial) oxidation are e.g. methanol or methane which can be converted to formic acid or formaldehyde. Waste materials which are subjected to oxidation, composting or storage are typically 20 domestic refuse, plastic wastes or packaging refuse. The organic substances are combusted mostly in customary combustion plants with air. The composting and storage of waste materials comprising organic substances generally proceed in refuse landfills. The exhaust gas or the exhaust air of such facili 25 ties can be treated advantageously by the method according to the invention. As organic substances for bacterial decomposition use is customarily made of stable manure, straw, liquid manure, clarified sewage sludge, fermentation residues and the like. The bacterial decomposition proceeds e.g. in customary biogas plants. The ex 30 haust air of such plants can advantageously be treated by the method according to the invention. The method is also suitable for the treatment of exhaust gases of fuel cells or chemical synthesis plants which make use of a (partial) oxidation of organic substances. 35 The fluid streams of the origin i), ii) or iii) above can have, for example, either the pres sure which roughly corresponds to the pressure of the ambient air, that is to say e.g. atmospheric pressure, or a pressure which deviates from atmospheric pressure by up to 1 bar. However, the fluid stream may also have a higher pressure.
    WO 2013/127765 PCT/EP2013/053775 5 Exhaust gases from combustion processes are preferred fluid streams to be treated according to the invention. 5 The fluid stream is brought into fluid-liquid contact with the absorption liquid in the ab sorption zone. The absorption zone may comprise any suitable apparatus, for example an absorption tower or an absorption column, e.g. a random packed column, arranged packing column, a tray column and/or in another absorber such as membrane contac tors, radial flow scrubbers, jet scrubbers, Venturi scrubbers and rotary spray scrubbers. 10 The fluid stream is preferably treated with the absorption liquid in an absorption column in countercurrent flow. The fluid stream in this case is generally fed into the lower re gion of the absorption zone and the absorption liquid into the upper region of the ab sorption zone. A treated fluid stream depleted of acid gases is formed and an absorp tion liquid loaded with acid gases is formed. 15 Water vapour contained in fluid stream condenses and/or becomes dissolved into the absorption liquid. Due to the limited solubility of water in the absorption liquid the water ultimately accumulates as a separate, aqueous phase within the absorption liquid. Preferably, separating the aqueous liquid comprises subjecting the loaded absorption 20 liquid to liquid-liquid phase separation to separate the aqueous liquid therefrom. The aqueous phase may be separated by at least one of decanting, and centrifuging. Mechanical coalescing techniques or electrocoalescing may be employed in order to obtain the aqueous liquid and the absorption liquid one another in cohesive form and 25 largely free of extraneous phase. For decanting, the bi-phase mixture can be introduced into a calming zone and be sep arated there. This is advantageously achieved in a horizontal, continuously operated phase separation vessel through which the mixture flows at a low flow velocity. Due to 30 the density difference between the phases, the mixture separates in the gravitational field. Separators having coalescence internals such as packing elements, coalescence surfaces or porous elements may suitably be used. The relative densities of the aqueous liquid and the absorption liquid will determine 35 which layer is upper and which is lower. The aqueous liquid will separate as upper lay er when the density of the absorption liquid is greater than that of the aqueous liquid. The aqueous liquid will separate as lower layer when the density of the absorption liq uid is smaller than that of the aqueous liquid.
    WO 2013/127765 PCT/EP2013/053775 6 The aqueous liquid separated from the absorption liquid is directed to a rehydration zone. In the rehydration zone, the treated fluid stream which is depleted of acid gases, is brought into fluid-liquid contact with the aqueous liquid. The rehydration zone may comprise any suitable apparatus for contacting a fluid and a liquid, for example a ran 5 dom packed column, arranged packing column, or a tray column. At least part of the aqueous liquid is volatilized and picked up by the treated fluid stream. Thus, the treated fluid stream acts as an outlet for at least part of the accumulated water. No significant additional energy expenditure is involved. 10 Suitably, the rehydration zone is arranged on top of the absorption zone. Thus, in a suitable embodiment the fluid stream is passed upwards through a tower including a lower portion containing the absorption zone for performing step b) and an upper por tion containing the rehydration zone for performing step c). 15 Generally, absorption of acid gases from the fluid stream into the absorption liquid is an exothermic process. Whether the exothermic heat is taken up by the absorption liquid or the treated fluid stream largely depends on the relative heat capacities of the ab sorption liquid and the fluid stream. Heat capacity is the product of mass flow M and specific heat capacity cp. Fig. 2a exemplifies the temperature profile in the absorption 20 zone in a situation where the heat capacity of the fluid stream is significantly greater than the heat capacity of the absorption liquid. The temperature of the treated fluid stream at the top of the absorption zone is higher than the temperature of the absorp tion liquid introduced at the top of the absorption zone and also higher than the tem perature of the fluid stream introduced at the bottom of the absorption zone. Fig. 2b 25 exemplifies the temperature profile in the absorption zone in a situation where the heat capacity of the absorption liquid is significantly greater than the heat capacity of the fluid stream. The temperature profile of Fig. 2a is characteristic of an acid gas removal application 30 where (M cp)fui/(M cp)absorption liquid > 0.5. This is typically the case for the treatment of fluids having low acid gas partial pressures, such as, e.g., combustion exhaust gases or low carbon dioxide natural gas. Low acid gas partial pressures result in absorption liquid circulation rates being low. The higher temperature of the treated fluid stream at the top of the absorption zone facilitates volatilization of the aqueous liquid in the rehy 35 dration zone and uptake of water vapour by the treated fluid stream. In preferred embodiments, the rehydration zone also acts as a scrubbing or backwash zone in order to transfer absorption liquid which is entrained by the treated fluid stream at least in part into the aqueous liquid. Emissions of the absorption liquid via the treated WO 2013/127765 PCT/EP2013/053775 7 fluid stream are avoided by scrubbing the treated fluid stream with the aqueous liquid. To exert a scrubbing action, the aqueous liquid must not be completely volatilized in step c). Spent aqueous liquid loaded with entrained absorption liquid may be collected at the bottom of the rehydration zone. The spent aqueous liquid may be circulated from 5 the bottom of the rehydration zone to the top thereof via a pump, in order to increase the hydraulic load of the rehydration zone for sufficient wetting and scrubbing. Addi tional feed water may be fed into the rehydration zone in order to improve the scrub bing efficiency. 10 At least part of the spent aqueous liquid may be recycled into the process, i.e., com bined with the bulk loaded absorption liquid or the bulk regenerated absorption liquid or both. In a preferred embodiment, the spent aqueous liquid is subjected to liquid-liquid phase 15 separation to obtain an aqueous phase and an entrained absorption liquid phase. At least part of the entrained absorption liquid phase may be recycled into the process, i.e., combined with the bulk loaded absorption liquid or the bulk regenerated absorption liquid or both. The aqueous phase may be discharged, e.g., sent to waste water treat ment. The volume of this aqueous phase is considerably smaller than the volume of the 20 aqueous liquid originally separated from the absorption liquid: Consequently, absorp tion liquid losses via the discharged aqueous phase would be decreased. From the absorption liquid which is loaded with the acid gas components, carbon diox ide and other acid gases can be liberated in a regeneration step, wherein a regenerat 25 ed absorption liquid is obtained. The resultant regenerated absorption liquid is subse quently recycled to the absorption zone. Expediently, regeneration of the loaded ab sorption liquid occurs by pressure release, heating, stripping or any combination there of. 30 Generally, the loaded absorption liquid is regenerated by heating, expansion, stripping with an inert fluid or a combination of two or all of these measures. Preferably, the loaded absorption liquid is regenerated in a stripper. The stripping gas required for the stripping is generated by partial evaporation of the absorption liquid in the bottom of the stripper. 35 In order to withdraw permanently from the earth's atmosphere the carbon dioxide which is eliminated, the carbon dioxide is customarily compressed and then forced into sub terranean deposits. In an embodiment of the process, the liberated acid gases are preferably fed into at least one compression unit. The compressed gases can then be WO 2013/127765 PCT/EP2013/053775 8 fed to a permanent storage (Carbon Capture and Storage, CCS)or used in enhanced oil recovery or enhanced gas recovery. Alternatively, the carbon dioxide may be sub jected to an industrial utilization such as urea synthesis or methanol synthesis (Carbon Capture and Utilization, CCU). 5 Before the regenerated absorption liquid is reintroduced into the absorption zone, it is cooled to a suitable absorption temperature. When the regeneration of the loaded ab sorption liquid involves heating of the loaded absorption liquid, it is preferred, in order to utilize the energy present in the hot regenerated absorption liquid, to preheat the 10 loaded absorption liquid from the absorber by heat exchange with the hot regenerated absorption liquid. By means of the heat exchange the loaded absorption liquid is brought to a higher temperature, and so in the regeneration step a lower energy input is required. By means of the heat exchange, also a partial regeneration of the loaded absorption liquid can proceed with liberation of acid gases. 15 The absorption liquid used in the process is incompletely miscible with water. Switcha ble ionic liquids are preferred absorption liquids. In suitable embodiments, the absorp tion liquid comprises a nitrogenous base and a weak acid. The nitrogenous base may be selected from amidines, guanidines and combinations thereof. The weak acid may 20 be selected from alcohols. Preferably, the nitrogenous base and the weak acid are se lected according to their limited miscibility with water. A suitable absorption liquid is a mixture of diazabicyclo[5.4.0]undec-7-ene (DBU) and 1-hexanol. The invention will be illustrated in more detail by the accompanying drawings. 25 Figure 1 shows an installation suitable for carrying out the method according to the invention. Figure 2a shows the temperature profile in the absorption zone in a situation where the 30 heat capacity of the fluid stream is significantly greater than the heat capacity of the absorption liquid. Fig. 2b shows the temperature profile in the absorption zone in a sit uation where the heat capacity of the absorption liquid is significantly greater than the heat capacity of the fluid stream. 35 According to figure 1, a fluid stream 1, e.g., a flue gas stream, is passed via blower 2 into the lower part of the absorption column 3 and brought into contact in countercur rent flow with an absorption liquid which is introduced via the line 16 into the upper re gion of the absorption column 3. The treated fluid stream depleted in carbon dioxide is fed via line 4 into a rehydration zone 5. An aqueous liquid is introduced in the rehydra- WO 2013/127765 PCT/EP2013/053775 9 tion zone 5 via the line 22. In the rehydration zone 5, entrained absorption liquid is eliminated from the treated fluid stream; also part of the aqueous liquid is volatilized and the treated fluid stream is saturated with water vapour. The treated fluid stream is removed from the rehydration zone 5 via the line 6. 5 The absorption liquid which is loaded with carbon dioxide is fed from the bottom of the absorption column 3 via line 7 to the decanter 8. An aqueous liquid accumulates as upper layer in decanter 8 and is withdrawn via line 22. Absorption liquid freed from the aqueous liquid separates as lower layer in decanter 8 and is fed via line 9, heat ex 10 changer 10 and line 11 to the stripper 12. In the bottom part of the stripper 12 the load ed absorption liquid is heated via a reboiler. As a result of the temperature elevation, the absorbed acid gases are converted back into the gas phase. The gas phase is re moved at the top of the stripper 12 and fed via line17 to the condenser 18. Absorption liquid which is condensed out is collected in the phase separator 19 and refluxed to the 15 stripper 12. The gaseous acid gases may be conducted to the compressor unit 20 and sent to sequestration via line 21. The regenerated absorption liquid 13 is recycled back to the absorption column 3 via the heat exchanger 10, line 14, the cooler 15, and line 16. 20 The spent aqueous liquid collected at the bottom of the rehydration zone 5 is sent via line 23 to the decanter 24. An aqueous phase accumulates as upper layer in decanter 24 and is discharged via line 26. Entrained absorption liquid separates as lower layer in decanter 24 and is combined via line 25 with the bulk of the regenerated absorption liquid withdrawn from the bottom of the stripper 12 via line 13. 25
    权利要求:
    Claims (13)
    [1] 1. A process for removing acid gases from a water vapour-containing fluid stream comprising 5 a) providing an absorption liquid which is incompletely miscible with water; b) treating the fluid stream in an absorption zone with the absorption liquid to obtain an acid gas-depleted treated fluid stream and an acid gas-loaded absorption liquid; 10 c) directing the treated fluid stream to a rehydration zone and treating the fluid stream with an aqueous liquid to volatilize at least part of the aqueous liq uid; d) regenerating the loaded absorption liquid to expel the acid gases at least in part and obtain a regenerated absorption liquid, and directing the regener 15 ated absorption liquid to step b); and e) separating, from the absorption liquid, an aqueous liquid that has con densed in the absorption zone, and directing the aqueous liquid to step c).
    [2] 2. The process according to claim 1, wherein separating the aqueous liquid com 20 prises subjecting the loaded absorption liquid to liquid-liquid phase separation to separate the aqueous liquid therefrom.
    [3] 3. The process according to claim 1 or 2, wherein the absorption liquid is essentially immiscible with water. 25
    [4] 4. The process according to any one of the preceding claims, wherein the aqueous liquid is incompletely volatilized in step c) so as to scrub the treated fluid stream with the aqueous liquid to remove entrained absorption liquid from the treated flu id stream. 30
    [5] 5. The process according to claim 4, wherein at least part of the spent aqueous liq uid is combined with the bulk loaded absorption liquid or the bulk regenerated absorption liquid or both. 35
    [6] 6. The process according to claim 4, wherein the spent aqueous liquid is subjected to liquid-liquid phase separation to obtain an aqueous phase and an entrained absorption liquid phase, and at least part of the entrained absorption liquid phase is combined with the bulk loaded absorption liquid or the bulk regenerated ab sorption liquid or both. WO 2013/127765 PCT/EP2013/053775 11
    [7] 7. The process according to any one of the preceding claims, wherein the fluid stream has an acid gases partial pressure of less than 2 bar. 5
    [8] 8. The process according to any one of the preceding claims, wherein the fluid stream is an exhaust gas from a combustion process.
    [9] 9. The process according to any one of the preceding claims, wherein regenerating the loaded absorption liquid occurs by pressure release, heating, stripping or any 10 combination thereof.
    [10] 10. The process according to any one of the preceding claims, wherein the loaded absorption liquid is preheated by indirect heat exchange with the regenerated ab sorption liquid. 15
    [11] 11. The process according to any one of the preceding claims, wherein the absorp tion liquid comprises a nitrogenous base and a weak acid.
    [12] 12. The process according to claim 11, wherein the nitrogenous base is selected 20 from amidines, guanidines and combinations thereof.
    [13] 13. The process according to claim 11 or 12, wherein the weak acid is selected from alcohols. 25
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    法律状态:
    2017-10-12| FGA| Letters patent sealed or granted (standard patent)|
    2020-09-24| MK14| Patent ceased section 143(a) (annual fees not paid) or expired|
    优先权:
    申请号 | 申请日 | 专利标题
    US201261605810P| true| 2012-03-02|2012-03-02||
    EP12157935.3||2012-03-02||
    US61/605,810||2012-03-02||
    EP12157935||2012-03-02||
    PCT/EP2013/053775|WO2013127765A1|2012-03-02|2013-02-26|Removing acid gases from water vapour-containing fluid streams|
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