A PROCESS FOR REMOVAL OF H2S FROM GASEOUS STREAMS WITH AMINO COMPOUNDS

Abstract: The removal of H₂S gas from a normally gaseous stream is accomplished with an absorbent solution containing a solvent and a nitrogen heterocyclic tertiary aminoalkanol or aminoetheralkanol or a tertiary amino azabicyclic alcohol or ether alcohol. In a preferred embodiment, the gaseous stream also contains CO₂, and the H₂S is selectively removed from the stream. The most preferred alcohol herein is tropine.

Description: This invention relates to an improved process for removal of H2S from normally gaseous streams wherein absorbent solutions of a certain class of heterocyclic amino compounds are employed. Preferably, the invention is directed to a process for selectively removing 1125 from gaseous mixtures containing H2S and C02 employing these absorbent solutions. The treatment of acid gas mixtures containing', inter alia, C02 and 1125 with aqueous amine solutions in an absorber tower typically results in the simultaneous removal of substantial amounts of both the C02 and H2S. For example, in one such process generally referred to as the aqueous amine process," relatively concentrated amine solutions are employed. A recent improvement on this process involves the use of sterically hindered amines to obtain nearly complete removal of acid gases such as CO 2 and H2S. This type of process may be used where the partial pressures of the C02 and related gases are low. Another process often used for speciali sed applications where the partial pressure of C02 is extremely high and/or where many acid gases are present, e.g.:, MZS, COS, C113511 and CS2, involves the use of an amine in combination with a physical absorbent;, generally referred to as the wnonaqueous solvent process. An improvement on this process involves the use of sterically hindered amines and organic solvents as the physical absorbent. It is often desirable', however', to treat acid gas mixtures containing both C02 and H2S so as to remove the H2S selectively from the mixture, thereby minimizing removal of the CO2. Selective removal of H2S results in a relatively high H25/C02 ratio in the separated acid gas which simplifies the conversion of 2S to elemental sulfur using the Claus process. The typical reactions of aqueous secondary and tertiary amines with C02 and 1125 can be represented as follows: EMI2.1 wherein R is an organic radical which may be the same or different and may be substituted with a hydroxyl group. The above reactions are reversible, and the partial pressures of both CO2 and 112S are thus important in determining the degree to which the above reactions occur. While selective 112S removal is applicable to a number of gas treating operations including treatment of hydrocarbon gases from shale pyrolysiS, refinery gas and natural gas having a low H2S/C02 ratio, it is particularly desirable in the treatment of gases wherein the partial pressure of H2S is relatively low compared to that of C02 because the capacity of an amine to absorb 1125 from the latter type gases is very low. Examples of gases with relatively low partial pressures of 1125 include synthetic gases made by coal gasification, sulfur plant tail gas and low-Joule fuel gases encountered in refineries where heavy residual oil is being thermally converted to lower molecular weight liquids and gases. Solutions of primary and secondary amines such as monoethanolamine (MEA)#, diethanolamine (DEA), dipropanolamine (DPA);, and hydroxyethoxyethylamine (DGA) are known to absorb both 1128 and CO2 gas. Diisopropanolamine (DIPA) is relatively unique among secondary aminoalcohols in that it has been used industrially, alone or with a physical solvent such as sulfolane, for selective removal of H2S from gases containing H2S and C02. The tertiary amine, methyldiethanolamine (MDEA), has a high degree of selectivity toward 1125 absorption over CO2-, but recently it was discovered that aqueous solutions of dialkylmonoalkanolamines, and particularly diethylmonoethanolamine (DEAE), have higher selectivity and capacity for H2S removal at higher loading levels than MDEA solutions. Other absorbent solutions which are selective to H2S removal include solutions of 1-formylpiperidine, piperazine, and solutions, in N-methyl-2-pyrrolidone, of cyanopyridine, an aromatic nitrile, an anhydride, or a piperazine. It has now been discovered that absorbent solutions of a certain class of amino compounds defined as either nitrogen heterocyclic tertiary aminoalkanols, nitrogen heterocyclic tertiary aminoetheralkanols, tertiary amino azabicyclic alcohols or tertiary amino azalicyclic ether alcohols have a high selectivity for H2S compared to C02. These amino compounds surprisingly maintain their high selectivity at high H2S and C02 loadings. In general, the present invention relates to a process for the removal of H2S from a normally gaseous stream by contacting said stream with an absorbent solution containing a solvent and an amino compound which is a nitrogen heterocyclic tertiary aminoalkanol, a nitrogen heterocyclic tertiary umlnoetheralkanol, a tertiary amino azabicyclic alcohol or a tertiary amino azabicyclic ether alcohol. In a preferred embodiment of the invention, the process involves the selective absorption of H2S from a normally gaseous stream also containing CO2 by contacting the stream with a solution of the amino compound above described in a solvent under conditions whereby H2S is selectively absorbed from the stream, wherein the amino compound is also characterized as having a pRa value at 200C greater than 8.6. The preferred solvents herein are water, a physical absorbent, preferably sulfolane, or a mixture thereof. In a still more preferred embodiment, after the contacting step whereby 112S is selectively absorbed from the stream, the absorbent solution containing the H2S is regenerated at least partially and the regenerated solution is recycled for selective absorption of H2S by recontacting it with the stream. Preferably, the regeneration step is carried out by heating and stripping the solution of any of its absorbed 112S and more preferably by heating and stripping the solution with steam. In the drawings Fig. 1 is a diagrammatic flow sheet illustrating an absorption-regeneration unit for selective removal of H2S from gaseous streams containing H2S and C02. Fig. 2 is a diagrammatic flow sheet illustrating an experimental sparged absorber unit for use in rapid determination of the selectivity of the amino compound for selective removal of H2S from gaseous streams containing HZS and C02 Fig. 3 graphically illustrates the selectivity for H2S plotted against the H2S and C02 loading for tropine and N-(3-hydroxypropyl)pyrrolidine (HPP) as compared to MDEA as control. Fig. 4 graphically illustrates the selectivity for H2S plotted against the 1125 and CO2 loading for 9-methyl-granatanin-3-ol and N-(3-hydroxypropyl)piperidine (HPPi). Fig. 5 graphically illustrates the selectivity for H2S plotted against the H2S and C02 loading for tropine and N-(3-hydroxypropyl)azetidine (HPA) as compared to DEAD, a non-cyclic aminoalkanol', as control. Fig. 6 graphically illustrates the selectivity for 1125 plotted against the 1125 and C02 loading for Nhydroxyethylpyrrolidine (HEP) and N-(2-hydroxyethoxyethyl) - pyrrolidine (HEEP) as compared to DEAE as control. Fig. 7 graphically illustrates the selectivity for H2S plotted against the 1125 and CO2 loading for N-(4-hydroxy-2-butyl)pyrrolidine (H2BP), N-(4-hydroxybutyl) pyrrolidine (HBP), N-(3-hydroxypropyl)piperidine (HPPi) and N-methyl-2-hydroxyethylpiperidine (MHEPi). Fig. 8 graphically illustrates the effect of the size of the heterocycle (n is number of ring atoms) on the selectivity for H2S plotted against the H2S and C02 load ingl, using N-(3-hydroxypropyl) azetidine, N-(3-hydroxy propyl)pyrrolidine#, N-(3-hydroxypropyl)piperidine and N-(3-hydroxypropyl)azepane. Fig. 9 graphically illustrates the effect of substitution of the heterocyclic ring by carbon on the selectivity for H2S plotted against the H2S and C02 loading!, using N-(3-hydroxypropyl)-2,5-dimethylpyrrolidine (HPDP) and N-(hydroxyethoxyethyl)-2,5-dimethylpyrrolidine (HEEDP). The nitrogen heterocyclic tertiary aminoalkanols or aminoetheralkanols of the present invention may be defined as compounds wherein the heterocycle portion contains 4-8 ring atoms', preferably 4-7 ring atoms, most preferably five ring atoms', of which one is nitrogen', and may be unsubstituted or substituted, e.g., with hydroxyl!, alkyl or hydroxyalkyl radicals, and wherein the alkanol portion is arranged in a linear or branched fashion', connected to the heterocycle portion via a ring nitrogen or ring carbon atom. The alkanol portion contains at least two carbon atomS, pref & ably 2-10 carbon atoms', when the alkanol carbon atom is attached to the nitrogen atom. The hydroxy carbon group can be attached directly to a ring carbon atom or separated from a ring carbon atom by 1-5 carbon atoms. The hydrocarbon chain of the alkanol portion may be al kox yla t i.e., may contain one or more ether oxygen atoms. The hydroxyl functionality of the alkanol chain may be primary or secondary. Representative such tertiary aminoalkanols and aminoetheralkanols include', for example', N-(3-hydroxy propyl) azetidine', N-hydroxyethylpyrrolidine', N-(3-hydroxy propyl)pyrrolidinei, N-(2-hydroxypropyl)pyrrolidine: :, N- (4-hydroxy-2-butyl) pyrrolidine., N-(4-hydroxybutyl) pyr- rolidinel, N-(hydroxyethoxyethyl)-2,5-dimethylpyrrolidine', N-(3-hydroxypropyl)-2,5-dimethylpyrrolidine, N-(3-hydroxypropyl)piperidine, N-hydroxyethylpiperidine, N-methyl-2 hydroxyethylpiperidine, N-methyl-3-hydroxymethylpiperidine', N-(2-hydroxyethoxyethyl)pyrrolidine, N-2- [ (2-hydroxy- propoxy)ethyllpyrrolidine-, N-2-[(2-hydroxypropoxy)pro- pyl) pyrrolidine1, N-(2-hydroxyethoxyethyl)piperidine, N-(3-hydroxypropyl)azepane., and the like. The other type of amino compounds applicable herein', namely, the tertiary amino azabicyclic alcohols or ether alcohols', may be defined as compounds wherein the two fused ring5, which share at least one side!, each have 4-10 ring atoms, preferably 4-7 ring atoms, of which one ring atom is nitrogen. Each ring may be unsubstituted or substituted, and the nitrogen atom forming the tertiary amino portion of the compound is situated within the bicyclic framework at a bridgehead or non-bridgehead ring position. The hydroxyl group(s) of the alcohol may be directly connected to the ring and/or may be connected to a hydrocarbon chain', preferably containing 2-10 carbon atoms, arranged in a linear or branched fashion and connected to the heterocycle via a ring nitrogen or a ring carbon atom. It is noted that the hydrocarbon chain may be alkoxylated, i.e., may contain one or more ether oxygen atoms. In the case where the hydroxyl group is attached to a hydrocarbon chain', it may be primary or secondary. Representatives of such azabicyclic alcohols and ether alcohols include, for example', tropine', pseudotro pine', 9-methylg ranatan in-3-ol-, isoquinucl idine ethanol!, trachelanthamidine, 4-hydroxymethylquinuclidine', Nhydroxyethylnortropine', N-hydroxyethyl (9-azabicyclo±3.3.l)- nonane), N-hydroxyethoxyethyl(9-azabicyclot4.2.1 ] nonane)t, 3-hydroxymethyl-8-methyl-8-azabicyclo[3.2.1]octane, and the like. The preferred amino compounds of this invention are N-(3-hydroxypropyl)azetidine;, N-hydroxyethylpyrrolidine', N-(3-hydroxypropyl)pyrrolidine', 9-methylgranatanin- 3-ol and tropine. The most preferred amino compound herein is tropine. The amino compounds used in the selective absorption process of the present invention llaually have a PKa value at 200C greater than 8.6, preferably greater than about 9.5 and more preferably the PKa value of the amino compound will range between about 9.5 and about 10.6. If the PKa is less than 8.6 the reaction with H2S is decreased, whereas if the PKa of the amino compound is much greater than about 10.6 an excessive amount of steam is required to regenerate the solution. Also, to ensure operational efficiency with minimal losses of the amino compound, the amino compound may have a relatively low volatility. For example', the boiling point of the amine (at 760 mm) may be typically greater than about 1800C, preferably greater than 2000C, and more preferably greater than 2250C. Another means for determining whether an amino compound is selective to H2S removal other than by measuring its PKa is by measuring its 15N nuclear magnetic resonance (NMR) chemical shift. By such measurements it has been found that the tertiary amino compounds herein may have a 15N NMR chemical shift greater than about #+50 ppm, preferably greater than about & 55 ppm, when a 90% by wt. amine solution in 10% by wt. D20 at 350C is measured by a spectrometet using liquid (neat) ammonia at 250C as a zero reference value. For example', tropine and N-(2-hydroxyethoxyethyl) pyrrolidine (HEEP) have 15N NMR chemical shift values of # +62.2 ppm and +53.2 ppni, respectively, whereas diethylmonoethanolamine (DEAE);, N-methyl-N-tertiarybutylaminoethoxyethanol, and methyldiethanol amine (MDEA) have 15N NMR chemical shift values of 6 + 43.7, # +45.0, and S +27.4 ppm', respectively. As evident from the data shown herein, those amino compounds measured having a 15N NMR chemical shift value greater than g +50 had a higher H2S selectivity than DEAE and MDEA having a 15N NMR chemical shift less than & ppm. The amino compounds herein may also be characterized by their high solubility in water at selective H2S removal conditions;, and most of the compounds are also generally soluble in polar organic solvent systems which may or may not contain water. The term 'absorbent solution" as used herein includes but is not limited to solutions wherein the amino compound is dissolved in a solvent selected from water or a physical absorbent or a mixture of water and physical absorbent. Solvents which are physical absorbents (as opposed to the amino compounds which are chemical absorbents) by definition function to solubilize the amino compounds and include', e.g., aliphatic acid aides', N-alkylated pyrrolidones, sulfone#, sulfoxides', glycols and the mono- and diethers thereof. The preferred physical absorbents herein are sulfones, and most particularly, sulfolane. The absorbent solution may have a concentration of amino compound of about 0.1 to 6 moles per liter of the total solution, and preferably 1 to 4 moles per liter', depending primarily on the specific amino compound employed and the solvent system utilized. If the solvent system is a mixture of water and a physical absorbent, the typical effective amount of the physical absorbent employed may vary from 0.1 to 5 moles per liter of total solution, and preferably from 0.5 to 3 moles per liter', depending mainly on the type of amino compound being utilized. The dependence of the concentration of amino compound on the particular compound employed is significant because increasing the.concentration of amino compound may reduce the basicity of the absorbent solution', thereby adversely affecting its selectivity for 1125 removal', particularly if the amino compound has a specific aqueous solubility limit which will determine maximum concentration levels within the range given above. It is important', therefore', that the proper concentration level appropriate for each particular amino compound be maintained to insure satisfactory results. The solution of this invention may include a variety of additives typically employed in selective gas removal processes., e.g.', antifoaming agents, antioxidants, corrosion inhibitors', and the like. The amount of these additives will typically be in the range that they are effective', i.e.', an effective amount. Also, the amino compounds described herein may be admixed with other amino compounds (i.e;, any amines other than those employed as amino compounds herein) as a blend, preferably with methyldiethanolamine, to form the absorbent solution. The ratio of the respective amino compounds may vary widely', for example', from 1 to 99 weight percent of the heterocyclic amino compounds described herein. Three characteristics which are of ultimate importance in determining the effectiveness of the amino compounds herein for 1125 removal are Wselectivitywt, 'loading' and 'capacity". The term "selectivity" as used throughout the specification is defined as the following mole ratio fraction: (moles of H9S/moles of C07) in liquid phase (moles of H2S/moles of C02) in gaseous phase The higher this fraction', the greater the selectivity of the absorbent solution for the H2S in the gas mixture. By the term 'loading' is meant the concentration of the 1125 and CO2 gases physically dissolved and chemically combined in the absorbent solution as expressed in moles of gas per mole of the amine. The best amino compounds are those which exhibit good selectivity up to a relatively high loading level. The amino compounds used in the practice of the present invention may have a 'selectivity' of not substantially less than 10 at a loading of 0.1 moles, preferably, a 'selectivity' of not substantially less than 10 at a loading of 0.2 or more moles of H2S and CO2 per mole of the amino compound. 'Capacity' is defined as the moles of 1125 loaded in the absorbent solution at the end of the absorption step minus the moles of H2S loaded in the absorbent solution at the end of the desorption step. High capacity enables one to reduce the amount of amine solution to be circulated and use less heat or steam during regeneration. The amino compounds herein are typically capable of reducing the H2S in gaseous mixtures to a relatively low level, e.g., less than about 200 ppm and typically have a relatively high capacity for H2S, e.g., greater than about 0.2 mole of H2S per mole of amine. The amino compounds may be characterized as having a kinetic selectivity" for H2S, 4.e., a faster reaction rate for 112S than for CO2 at absorption conditions. In addition they may be characterized as having a higher capacity for H2S at equivalent kinetic selectivity for 1125 over CO2. This higher capacity results in the economic advantage of lower steam requirements during regeneration. The normally gaseous stream herein necessarily includes H2S, ordinarily in gaseous form. (The term 'normally" refers to ambient conditions of temperature and pressure.) It may optionally include other gases such as CO2, N2 CH4, H21 CO, H2O, COS, HCN,#C2H41 NH31 and the like. Often such gas mixtures are found in combustion gases, refinery gases, town gas, natural gas, syn gas, water gas, propane, propylene, heavy hydrocarbon gases, etc. The absorbent solution herein is particularly effective when the gaseous mixture is a gas, obtained, for example, from shale oil retort gas, coal or gasification of heavy oil with air/steam or oxygen/steam, thermal conversion of heavy residual oil to lower molecular weight liquids and gases, or in sulfur plant tail gas clean-up operations. The absorption step of this invention generally involves contacting the normally gaseous stream with the. absorbent solution in any suitable contacting vessel. In such processes, the normally gaseous mixture from which the H2S is to be removed may be brouqht into intimate contact with the absorbent solution using conventional means, such as a tower or vessel packed with, for example, rings or with sieve plates, or a bubble reactor. In a typical mode of practising the invention wherein H2S is selectively absorbed from a mixture also containing Co2r the absorption step is conducted by feeding the normally gaseous mixture into the lower portion of the absorption tower while fresh absorbent solution is fed into the upper region of the tower. The gaseous mixture, freed largely from the H2S, emerges from the upper portion of the tower, and the loaded absorbent solution, which contains the selectively absorbed H2S, leaves the tower near or at its bottom. Preferably, the inlet temperature of the absorbent solution during the absorption step is in the range of from about 20 to about 1000C, and more preferably from 40 to about 600C. Pressures may vary widely; acceptable pressures are between 0.4 and 140.6 kg/cm2, preferably 1.4 and 105.5 kg/cm2, and most preferably 1.8 and 70.3 kg/cm2 in the absorber. The contacting takes place under conditions such that the H2S is selectively absorbed by the solution. The absorption conditions and apparatus are designed so as to minimize the residence time of the liquid in the absorber to reduce CO2 pickup while at the same time maintaining sufficient residence time of gas with liquid to absorb a maximum amount of the H28 gas. The amount of liquid required to be circulated to obtain a given degree of H2S removal will depend on the chemical structure and basicity of the amino compound and on the partial pressure of H2S in the feed gas. Gas mixtures with low partial pressures such as those encountered in the thermal gas conversion process will require more liquid under the same absorption conditions than gases with higher partial pressures such as shale oil retort gases. A typical procedure for the selective H2S removal phase of the process comprises selectively absorbing H2S via countercurrent contact of the gaseous mixture containing H2S and CO2 with the solution of the amino compound in a column containing a plurality of trays at a low temperature, e.g., below 450C, and at a gas velocity of at least about 9.1 cm/sec (based on "active" or aerated tray surface), depending on the operating pressure of the gas, said tray column having fewer than 20 contacting trays, with, e.g., 4-16 trays being typically employed. Alternatively, packed beds may be used in place of trays. After contacting the normally gaseous mixture with the absorbent solution, which becomes saturated or partially saturated with H2S, the solution may be at least partially regenerated so that it may be recycled back to the absorber. As with absorption, the regeneration may take place in a single liquid phase. Regeneration or desorption of the acid gases from the absorbent solution may be accomplished by conventional means such as pressure reduction of the solution or increase of temperature to a point at which the absorbed H25 flashes off, or by passing the solution into a vessel of similar construction to that used in the absorption step, at the upper portion of the vessel, and -passing an inert gas such as air or nitrogen or preferably steam upwardly through the vessel. The temperature of the solution during the regeneration step should be in the range from about 50 to about l700C, and preferably from about 80 to 1200C, and the pressure of the solution on regeneration should range from about 0.04 to about 7.0 kg/cm2, preferably 0.07 to about 3.5 kg/cm2. The absorbent solution, after being cleansed of at least a portion of the H2S gas, may be recycled back to the absorbing vessel. Makeup absorbent may be added as needed. In the preferred regeneration technique, the H2S-rich solution is sent to the regenerator wherein the absorbed components are stripped by the steam which is generated by re-boiling the solution. Pressure in the flash drum and stripper is usually 0.07 to about 3.5 kg/cm2, preferably 1.05 to about 2.1 kg/cm2, and the temperature is typically in the range from about 50 to 1700C, preferably about 80 to l200C. Stripper and flash temperatures will, of course, depend on stripper pressure; thus at about 1.05 to 2.1 kg/cm2 stripper pressures, the temperature will be about 80 to about l200C during desorption. Heating of the solution to be regenerated may very suitably be effected by means of indirect heating with low-pressure steam. It is also possible, however, to use direct injection of steam. In one embodiment for practising the entire process herein, as illustrated in Figure 1, the gas mixture to be purified is introduced through line 1 into the lower portion of a gas-liquid countercurrent contact ing column 2, said contacting column having a lower section 3 and an upper section 4. The upper and lower sections may be segregated by one or a plurality of packed beds as desired. The absorbent solution as described above is introduced into the upper portion of the column through a pipe 5. The solution flowing to the bottom of the column encounters the gas flowing countercurrently and dissolves the H2S preferentially. The gas freed from most of the H2S leaves through a pipe 6 for final use. The solution, containing mainly 1125 and some CO2, flows toward the bottom portion of the column, from which it is discharged through pipe 7. The solution is then pumped via pump 8 through an optional heat exchanger and cooler 9 disposed in pipe 7, which allows the hot solution from the regenerator 12 to exchange heat with the cooler solution from the absorber column 2 for energy conservation. The solution is entered via pipe 7 to a flash drum 10 equipped with a line (not shown) which vents to line 13 and then introduced by pipe 11 into the upper portion of the regenerator 12, which is equipped with several plates and effects the desorption of the H2S and CO2 gases carried along in the solution. This acid gas mixture is passed through a pipe 13 into a condenser 14 wherein cooling and condensation of water and amine solution from the gas- occur. The gas then enters a separator 15 where further condensation is effected The condensed solution is returned through pipe 16 to the upper portion of the regenerator 12. The gas remaining from the condensation, which contains H2S and some CO2, is removed through pipe 17 for final disposal (e.g., to a vent or incinerator or to an apparatus which converts the H2S to sulfur, such as a Claus unit or a Stretford conversion unit (not shown)). The solution is liberated from most of the gas which it contains while flowing downward through the regenerator 12 and exits through pipe 18 at the bottom of the regenerator for transfer to a reboiler 19. Reboiler 19, equipped with an external source of heat (e.g., steam is injected through pipe 20 and the condensate leaves through a second pipe (not shown))1, vaporizes a portion of this solution (mainly water) to drive further 1125 there from. The H2S and steam driven off are returned via pipe 21 to the lower section of the regenerator 12 and leave through pipe 13 for entry into the condensation stages of gas treatment. The solution remaining in the reboiler 19 is drawn through pipe 22, cooled in heat exchanger 9, and introduced via the action of pump 23 (optional if pressure is sufficiently high) through pipe 5 into the absorber column 2 The amino compounds herein are found to be superior to those used in the past, particularly to MDEA and DEAE, in terms of both selectivity and capacity for maintaining selectivity over a broad loading range. Typically, a gaseous stream to be treated having a 1:10 mole ratio of HzS:CO2 from an apparatus for thermal conversion of heavy residual oil!, or a Lurgi coal gas having a mole ratio of H2S:CO2 of less than 1:10 will yield an acid gas having a mole ratio of H2S:CO2 of about 1:1 after treatment by the process of the present invention. The process herein may be used in conjunction with another H2S selective removal process; however, it is preferred to carry out the process of this invention by itself, since the amino compounds are extremely effective by themselves in preferential absorption of H2S. The invention is illustrated further by the following examples, which', however, are not to be taken as limiting in any respect. All parts and percentages', unless expressly stated to be otherwise', are by weight. Also, the PKa values were obtained at 200C unless otherwise noted. The abbreviation b.p. means boiling point. EXAMPLE 1 Preparation of N-(3-hydroxypropyl) azetidine To 14.4 g of LiAlH4 in 270 ml of tetrahydrofuran was added 99 g of ethyl-3-(N-azetidinyl)propionate dissolved in 90 ml of tetrahydrofuran at a rate sufficient to maintain a gentle reflux. After an additional one-hour reflux the reaction mixture was cooled and treated sequentially with 14 ml of 1120 and 14 ml of 12.5% NaOH. Filtration and distillation yielded 35.7 g of N-(3-hydroxypropyl)azetidine (b.p. = 94.6 C at 20 mm; analysis for C6H13 NO, calculated: %N = 12.16; found: %N = 12.10). EXAMPLE 2 Preparation of N-(3-hydroxypropyl) azepane A solution of 1 mole of azepane and 0.5 mole of 3-chloro-l-propanol in 500 ml of ethanol was refluxed for 18 hours. The reaction mixture was treated with 0.55 mole of KOH and reflexed for 0.75 hour. Coolingt filtration and distillation yielded 88% of N-(3-hydroxypropyl)azepane (b.p. = l36 C at 21 mm; analysis for C9H19N(Y, calculated: %N = 8.91; found: %N = 8.30). EXAMPLE 3 Preparation of N-(3-hydroxypropyl) 2, 5-dimethylpyrrolidine A total of 3 mole of 2,5-hexanedione', 3 moles of 3-amino-1-propanolr, , 10 g of 10% Pd/C, and 500 ml of ethanol were charged to an autoclave. The reaction mixture was pressured up to 77.3 kg/cm2 of 112 and kept for 3 hours at 100 C. Distillation yielded 170 g of N-(3-hydroxy propyl)-2,5-dimethylpyrrolidine (b.p. = 1190C at 25 mm). EXAMPLE 4 Preparation of N- (hydroxyethoxyethyl) - 2,5-dimethylpyrrolidine A solution of 0.95 mole of Z,5-hexanedionew, 0.95 mole of diglycolamine', and 1.4 g of p-toluenesulfonic acid in 400 ml of toluene was refluxed in a flask fitted with a Dean Stark trap. After removal of the required amount of water, distillation yielded 157 g of N-(hydroxyethoxy ethyl)-2,5-dimethylpyrrole with b.p. = 110 C at 13 mm. The pyrrole, 0.8 mole in 1.2 1 of ethanol:, was hydrogenated at 77.3 kg/cm2 H2 for three hours at 1000C using 5 g of 10% Pd/C. The cooled reaction mixture was filtered and distilled to yield N-(hydroxyethoxyethyl) 2,5-dimethylpyrrolidine (b.p. = 800C at 0.4 mm). EXAMPLE 5 Selective H2S Removal from a Mixture Containing 1195 and CO2 Fig. 2 illustrates the sparged absorber unit, operated on a semi-batch mode, used to evaluate the selectivity for H2S removal of the amino compounds of the invention herein. A gas mixture comprised of 10% CO2, 1% H2S and -8'9% N2, expressed in volume percent, respectively, was passed from a gas cylinder (not shown) through line 30 to a meter 31 measuring the rate at which the gas is fed to the absorber. For all examples this rate was 3.6 liters per minute. The gas was then passed through line 32 to a gas chromatography column (not shown) continuously monitoring the composition of the inlet gas and through lines 33 and 34 to a sparged absorber unit 35, which is a cylindrical glass tube 45 cm high and 3.1 cm in diameter charged with 100 ml of the absorbent amine solution 36. The gas was passed through the solution at a solution temperature of 400C, and 10-ml samples of the solution were periodically removed from the bottom of the absorber unit through lines 34 and 37 to be analyzed for H2S and CO2 content. The H2S content in the liquid sample was determined by titration with silver nitrate. The CO2 concent of the liquid sample was analyzed by acidifying the sample with an aqueous solution of 10% HC1 and measuring the evolved CO2 by weight gain on NaOHcoated asbestos. While the solution was being periodically withdrawn from the bottom of the absorber unit, the gas mixture was removed from the top thereof via line 38 to a trap 39 which served to scrub out any H2S in the outlet gas. The resulting gas could optionally then be passed via lines 40 and 41 for final disposal or via line 42 to a gas chromatography column (not shown) for periodic evaluation of the composition of the outlet gas to check for system leaks. For purpose, of the examples, the 1125 and CO2 contents of the inlet gas phase were measured, and the H2S and and CO2 contents of the liquid phase were determined as described above. These data were used to calculate selectivity values of the amine as defined above, which were plotted as a function of the loading of the absorbent solution with 112S and COZI in units of moles acid gas per mole of the amino compound. The above procedure was employed using as the absorbent solution aqueous 3M solutions of tropine (PKa = 10.3, b.p. = 233 C)I, N-(3-hydroxypropyl)pyrrolidine (HPP) (PKa '= 10.21, b.p. = 10300 at I3 mm) and methyldiethanolamine (MDEA) as control. The selectivity plots, given in Fig. 3, compare the H2S selectivities achieved using an azabicyclic alcohol (tropine), a similarly structured monocyclic aminoalkanol (HPP) and an acyclic alcohol (MDEA). From the plots it is seen that tropine and HPP have a far greater selectivity than MDEA, both at low and high C02 and H2S loadings but particularly at the higher H2S and C02 loadings where MDEA has negligible selectivity. The data in Fig. 3 also show that the amino compounds of the present invention have very high capacity for both H2S and C02 compared to methyldiethanolamine (MDEA) in addition to high 112S selectivities. It will be apparent from an inspection of the data in Fig. 3 that if the absorption process is conducted under conditions such that. the amino compound has a long contact time with the gases to be absorbed', the selectivity for H2S decreases, but the overall capacity for both CO2 and HS remains rather high. Therefor, one may, in some instance, wish to carry out a wnon-selectivew absorption process to take advantage of the large absorption capacity of the amino compounds of the invention. Acco-rdingly, one may carry out a wnon-selectivew acid gas removal absorption process using the amino compounds of the invention. Such Wnon-selectivew processes are particularly useful in scrubbing natural gases which contain relatively high levels of H2S and low to nil levels of CO2. As such, the amino compounds of the invention may replace some or all of monoethanolamine (ME?) or diethanolamine (DEA) commonly used or such scrubbing processes. EXAMPLE 6 The procedure of Example 5 was repeated using as the absorbent solution aqueous 3M solutions of 9-methylgranatanin-3-ol (PKa = 9.9, m.p. = 920C, b.p. = about 25000 at 760 mm) and N-(3-hydroxypropyl)piperidine (HPPi). The selectivity plots are given in Fig. 4. EXAMPLE 7 The procedure of Example 5 was repeated using as the absorbent solution aqueous 3M solutions of tropine!, N-(3-hydroxypropyl)azetidine (HPA) (as prepared in Example 1)', and diethylmonoethanolamine (DEAE) (as a control). Their selectivity plots, given in Fig. S, show the superior selectivity for H2S of tropine and HPA over an acyclic aminoalcohol. From the selectivity plots shown in Figs. 3, 4, and 5 it is apparent that tropine', an azabicyclic alcohol', exhibits even better selectivity performance than the monocyclic aminoalkanols', HPF, RPPi and HPA. EXAMPLE 8 The procedure of Example 5 was repeated using as the absorbent solution aqueous 3M solutions of N-hydroxyethylpyrrolidine (HEP) (PKa = 9.95, b.p. = 8000 at 13 mm)#, N-(2-hydroxyethoxyethyl)pyrrolidine (BEEP ) (PKa = 9.9So b.p = 11000 at 5 mm) and diethylmonoethanolamine (DEAE) as control. From the three selectivity plots shown in Fig. 6 it is .apparent that HEP and HEEP are much more selective than DEAE and are even more selective at higher H2S and C02 loadings where DEAE has poorer selectivity. Also, it is apparent that O-alkoxylation does not adversely affect the ability of the aminoalkanol to absorb 1128 selectively. EXAMPLE 9 The procedure of Example 5 was repeated using as the absorbent solution aqueous 3M solutions of one of four amines, i.e., N-(4-hydroxy-2-butyl')pyrrolidine (H2BP) (PKa = 10.25 b.p. = 9800 at 7 mm), N-(4-hydroxybutyl) pyrrolidine (HBP) (PKa = 10.21', b.p. = 9500 at 2 mm), N-(3-hydroxypropyl)piperidine (HPPi) (PKa = 10.2, b.p. = 9700 at 5 mm)', and N-methyl-2-hydroxyethylpiperidine (MHEPi) (PKa = 9.90, b.p. = 23300 at 760 mm). A selectivity plot for each amine was recorded, as shown in Fig. 7. It can be seen that HMP is the best of the four in terms of both selectivity and maintenance of capacity. However;, all four amines showed better selectivity at the loading ranges tested than both MDEA and DEAE illustrated in Figs. 3 and C, respectively. EXAMPLE 10 The procedure of Example 5 was repeated using as the absorbent solution aqueous 3M solutions of one of four N-(3-hydroxypropyl)-substituted heterocycles wherein the heterocycle contained 4, 5, 6 or 7 ring atoms', namely, N-(3-hydroxypropyl)azetidine (prepared as described above), N-(3-hydroxypropyl)pyrrolidine., N-(3-hydroxypropyl)piperidine and N-(3-hydroxypropyl)azepane (prepared as described above). From the selectivity plots shown in Fig. 8 it is apparent that decrease in ring size improves the selectivity of the aminoalkanol for the 112S, with the azetidinyl compound being the best of the four. EXAMPLE 11 The procedure of Example 5 was repeated using as the absorbent solution aqueous 3M solutions of N-(3hydroxypropyl)-2,5-dimethylpyrrolidine (HPDP) and N (hydroxyethoxyethyl)-2,5-dimethylpyrrolidine (HEEDP). The two selectivity plots are shown in Fig. 9. EXAMPLE 12 Table 1 shows the effect of 0-alkoxylation of the heterocyclic aminoalkanols on their boiling points and PKa values. It can be seen that in each case the boiling points increase relative to the respective parent compound while the PKa remains constant. In addition to their low volatility and suitable basicity, the alkoxylated aminoalkanols exhibit a solubility in water ( > 3M) which is comparable or identical to that of the parent aminoalkanol. Table 1 Aminoalkanol PKa Boiling Point, OC (mm) EMI20.1 9.95 80 (13) 9.95 110 (5) 10.20 101 (13) 10.20 140 (20) 10.20 75 (14) 10.20 100 (1) while all examples herein illustrate the superior performance of the amino compounds for selective 112S removal using an absorber unit as represented by Fig. Z, it will also be possible to achieve effective selective 112S removal by using the amino compounds in an absorptionregeneration unit as depicted in Fig. 1. In summary, this invention is seen to provide a special class of amino compounds characterized as nitrogen heterocyclic tertiary aminoalkanols and aminoetheralkanols and tertiary amino azabicyclic alcohols or ether alcohols having a high selectivity for 1125 in preference to coal which selectivity is maintained at high 1125 and C02 loading levels.

Claims: CLAIMS: 1. A process for removing H2-S fr-om a normally gaseous stream which comprises contacting said stream with an absorbent solution containing a solvent and an amino compound wherein the amino compound is a nitrogen heterocyclic tertiary aminoalkanol, a nitrogen heterocyclic tertiary aminoetheralkanol, a tertiary amino azabicyclic alcohol or a tertiary amino azabicyclic ether alcohol. 2. A process according to claim 1 wherein the normally gaseous stream also contains C02 and H2S is selectively absorbed from the stream. 3. A process according to either of claims 1 and 2 wherein the amino compound has a pKa value at 200C of greater than 8.6. 4. A process according to any one of claims 1 to 3 wherein the solvent is water, a physical absorbent, or a mixture thereof. 5. A process according to any one of claims 1 to 4 wherein the total concentration of amino compound in the absorbent solution is in the range of from about 0.1 to 6 moles per litre. 6. A process according to any one of claims 1 to 5 which is conducted at a temperature ranging from about 20 to 1000C and at a pressure ranging from 0.4 to 140.6 kg/cm2, the absorbent solution is regenerated by heating at a temperature ranging from 50 to about 1700C and at a pressure ranging from 0.07 to about 3.5 kg/cm2 and by stripping the solution of its absorbed H2S. 7. A process according to any one of claims 1 to 6 wherein the amino compound is N-(3-hydroxypropyl)azetidine, N-hydroxyethylpyrrolidine, N- (3-hydroxypropyl )pyrrolidine or 9-methyigranatanin-3-ol. 8. A process according to any one of claims 1 to 6 wherein the amino compound is tropine. 9. An absorbent solution comprising a solvent, an amino compound, said amino compound being a nitrogen heterocyclic tertiary aminoalkanol, a nitrogen heterocyclic tertiary aminoetheralkanol, a tertiary amino azabicyclic alcohol or a tertiary amino azabicyclic ether alcohol. 10. A solution according to claim 9 wherein the solvent is a physical absorbent.

Inventors: SARTORI, GUIDO, SAVAGE, DAVID WILLIAM, STOGRYN, EUGENE LEO
Applicants: EXXON RESEARCH AND ENGINEERING COMPANY
Application year: 1983
Main classification: B01D53
IPC codes: B01D53