A PROCESS FOR REMOVING ACID GASES USING A BASIC SALT ACTIVATED WITH A NON-STERICALLY HINDERED DIAMINO COMPOUND

Abstract: Acidic gases containing carbon dioxide are removed from a normally gaseous mixture by absorbing CO₂ from the gaseous mixture with an aqueous solution comprising a basic alkali metal salt or hydroxide and an activator or promoter system for the salt or hydroxide which contains (i) at least one non-sterically hindered diamino compound defined as a diamine having both a primary and a tertiary amino moiety wherein the primary amino moiety is attached to a primary carbon atom or as a diaminoalcohol having a tertiary amino moiety separated by four methylene groups from a primary amino moiety and having at least one hydroxyl group, and (ii) an amino acid, and desorbing at least partially the absorbed CO₂ from the aqueous solution.

Description: A PROCESS FOR REMOVING ACID GASES USING A BASIC SALT ACTIVATED WITH A NON-STERICALLY HINDERED DIAMINO COMPOUND This invention relates to use of a specific class of diamino compounds in admixture with an amino acid as cosolvent therefor in an aqueous absorbing solution for "hot pot" type acid gas scrubbing processes. Recently, it was shown in U.S. Patent No. 4,112,050 that sterically hindered amines are superior to diethanolamine (DEA) as promoters for alkaline salts in the "hot pot" acid gas scrubbing process. U.S. Patent No. 4,094,957 describes an improvement to this process whereby amino acids, particularly sterically hindered amino acids, serve to prevent phase separation of the aqueous solution containing sterically hindered amines at high temperatures and low fractional conversions during the acid gas scrubbing process. While combinations of sterically hindered diamines such as N-cyclohexyl propanediamine (CHPD) with a cosolvent such as pipecolinic acid represent preferred activator systems in U.S. Patent No. 4,094,957 for promoting hot carbonate CO2 scrubbing operations, there are certain disadvantages associated therewith. One difficulty is that sterically hindered primary-secondary diamines such as CHPD are unstable in the presence of C02 and tend to enter into undesirable intramolecular condensation reactions therewith to form a cyclic urea precipitate, which reactions are catalyzed by any H2S present in the gaseous system. The side reaction of CHPD with C02 can be represented as follows: EMI1.1 Not only is the diamine consumed by this reaction, but the insoluble cyclic urea must be removed from the system to avoid congestion of the plant operation. It has been discovered that a certain family of non-sterically hindered diamino compounds including diamines and diaminoalcohols are stable in the presence of the gaseous mixture and, together with an amino acid cosolvent, form an amino activator system which performs effectively in hot carbonate scrubbing operations. The diaminoalcohols, characterized as containing at least one hydroxyl group and a tertiary amino group separated by four methylene groups from a primary amino group, in addition to having the above properties, are also non volatile. Closely analogous diaminoalcohols having three methylene groups between the amino groups were found to be unstable in the presence of CO2 and H2S. In one embodiment of the present invention there is provided a process for the removal of CO2 from a gaseous stream containing CO2 which comprises (1) in an absorption step, absorbing CO2 from said gaseous stream with an aqueous absorbing solution comprising (a) a basic alkali metal salt or hydroxide selected from alkali metal bicarbonates, carbonates, hydroxides, borates, phosphates, and their mixtures, and (b) an activator or promoter system for said basic alkali metal salt or hydroxide comprising (i) at least one non-sterically hindered diamino compound which is defined as a diamine containing both a primary and a tertiary amino moiety wherein the primary amino moiety is attached to a primary carbon atom or as a diaminoalcohol containing a tertiary amino moiety separated by four methylene groups from a primary amino moiety and containing at least one hydroxyl group, and (ii) an amino acid which has the capability to increase the solubility of said diamino compound in alkaline aqueous conditions at elevated temperatures, and (2) in a desorption and regeneration step, desorbing at least a portion of the absorbed CO2 from said absorbing solution. As another embodiment of the invention there is provided an aqueous acid gas scrubbing composition comprising: (a) 10 to about 40% by weight of an alkali metal salt or hydroxide, (b) 2 to about 20% by weight of a diamino compound as specified above, (c) 2 to about 20% by weight of an amino acid which has the capability to increase the solubility of the diamine in alkaline aqueous conditions at elevated temperatures and (d) the balance, water. The mole ratio of diamino compound to amino acid may vary widely but is preferably 1:3 to 3:1, most preferably 1:1. The amino acid may be added to the scrubbing solution containing the diamino compound all at once or in increments during the gas scrubbing operation. The non-sterically hindered diamino compound herein is water soluble in the presence of the amino acid co-promoter and is a diamine or diaminoalcohol having the structural characteristics indicated below. The diamine has both a primary and tertiary amino moiety, provided that the primary amino moiety is attached to a primary carbon atom. A preferred diamine of the invention is a compound represented by the following general formulae: EMI3.1 wherein R and R' independently represent a C1 - C6 alkyl or a C6 - Cg cycloalkyl group, n is an integer of at least 2, and m is an integer of at least 4. Typical such diamines include N,N-diethyl-l,3-propanediamine, N-methyl-N-butyl-1,3-propanediamine, N,N-dibutyl-1,3propanediamine, N-methyl-N-cyclohexyl-l,3-propanediamine, N-methyl-N-cyclohexyl ethylenediamine, N-3-aminopropyl2-pipecoline, N-(2-aminoethyl)-hexamethyleneimine, N-(3-aminopropyl)-hexamethyleneimine, and the like. Preferably, the diamine will have a cyclic tertiary amino moiety, and most preferably will be N-3-aminopropyl2-pipecoline. The diamino compound may also be a non-sterically hindered diaminoalcohol which has at least one hydroxyl group and a tertiary amino group separated by four methylene groups from a primary amino group. A preferred diaminoalcohol herein is represented by the following general formula: H2N - (CH2)4 - NRR' wherein R and R' each independently represent a C1 - C6 alkyl group and either R or R' or both R and R' have a terminal or pendant hydroxyl group. Typically, such diaminoalcohols include N-(2-hydroxyethyl)-N-(n-propyl)1, 4-butanediamine, N- (2-hydroxyethyl) -N- (isopentyl) - 1,4-butanediamine, N,N-di(2-hydroxyethyl)-l,4-butane- diamine, N-(2-hydroxypropyl)-N-methyl-l,4-butanediamine, and the like. The preferred diaminoalcohols herein are those containing only one hydroxyl group, and most preferred is N-(2-hydroxyethyl)-N-(n-propyl)-l,4-butane- diamine. The amino acids herein include any amino acids which are soluble in the alkaline aqueous solution to be used in the acid gas treating solution. Preferably, the amino acid will have 4 to 8 carbon atoms and one amino moiety and will be free of any hydroxyl groups. Especially preferred within this category are tertiary amino acids, defined as amino acids wherein the amino moiety is a tertiary amino moiety such as N,N-dimethyl glycine and N,N-dietbyl glycine. Also especially preferred are sterically hindered amino acids of 4 to 8 carbon atoms defined as those containing at least one secondary amino moiety attached to either a secondary or tertiary carbon atom or a primary amino moiety attached to a tertiary carbon atom. At least one of the nitrogen atoms will have a sterically hindered structure. Typical sterically hindered amino acids useful in the practice of the present invention will include N-secondary butyl glycine, pipecolinic acid, N-isopropyl glycine, N-2-amyl glycine, N-isopropyl alanine, N-secondary butyl alanine, 2-amino-2 methyl butyric acid, and 2-amino-2-methyl valeric acid. In general, the aqueous scrubbing solution will comprise an alkaline material comprising a basic alkali metal salt or alkali metal hydroxide selected from Group IA of the Periodic Table of Elements. More preferably, the alkali metal salt or hydroxide in the scrubbing solution is potassium or sodium borate, carbonate, hydroxide, phosphate, or bicarbonate or mixtures thereof. Most preferably, the alkaline material is potassium carbonate. The alkaline material comprising the basic alkali metal salt or alkali metal hydroxide may be present in the scrubbing solution in the range from about 10% to about 40% by weight, preferably from 20% to about 35% by weight. The actual amount of alkaline material chosen will be such that the alkaline material and the activator or promoter system remain in solution throughout the entire cycle of absorption of CO2 from the gas stream and desorption of CO2 from the solution in the regeneration step. likewise, the amount and mole ratio of the amino acid to the diamine is maintained such that they remain in solution as a single phase throughout the absorption and regeneration steps. Typically, these criteria are met by including from about 2 to about 20% by weight of the amino acid, preferably from 5 to 15% by weight, more preferably, 5 to 10% by weight of the amino acid and from 2 to about 20% by weight, preferably, 5 to about 15% by weight, of the non-sterically hindered diamino compound. The aqueous scrubbing solution may include a variety of additives typically used in acid gas scrubbing 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. Fig. 1 is a diagrammatic flow sheet illustrating an experimental reaction apparatus for removing carbon dioxide from gaseous streams. The term acid gas includes CO2 alone or in combination with H2S, CS2, HCN, COS and the oxides and sulfur derivatives of C1 to C4 hydrocarbons. These acid gases may be present in trace amounts within a gaseous mixture or in major proportions. In the absorption step, the contacting of the absorbent mixture and the acid gas may take place in any suitable contacting tower. In such processes, the gaseous mixture from which the acid gases are to be removed may be brought into intimate contact with the absorbing solution using conventional means, such as a tower packed with, for example, ceramic rings or with bubble cap plates or sieve plates, or a bubble reactor. In a preferred mode of practising the invention, the absorption step is conducted by feeding the gaseous mixture into the base of the tower while fresh absorbing solution is fed into the top. The gaseous mixture freed largely from acid gases emerges from the top. Preferably, the temperature of the absorbing solution during the absorption step is in the range from about 25 to about 2000C, and more preferably from 35 to about 1500C. Pressures may vary widely; acceptable pressures are between 5 and 2000 psia, preferably 100 to 1500 psia, and most preferably, 200 to 1000 psia in the absorber. In the desorber, the pressures will range from about 5 to 100 psig. The partial pressure of the acid gas, e.g., CO2, in the feed mixture will preferably be in the range from about 0.1 to about 500 psia, and more preferably in the range from about 1 to about 400 psia. The contacting takes place under conditions such that the acid gas, e.g., C02, is absorbed by the solution. Generally, the countercurrent contacting to remove the acid gas will last for a period of from 0.1 to 60 minutes, preferably 1 to 5 minutes. During absorption, the solution is maintained in a single phase. The amino acid aids in reducing foam in the contacting vessels. The aqueous absorption solution comprising the alkaline material and the activator system of diamine and amino acid which is saturated or partially saturated with gases, such as CO2 and H2S, may be regenerated so that it may be recycled back to the absorber. The regeneration should also take place in a single liquid phase. Therefore, the presence of the amino acid cosolvent provides an advantage in this part of the overall acid gas scrubbing process. The regeneration or desorption is accomplished by conventional means, such as pressure reduction, which causes the acid gases to flash off by passing the solution into a tower of similar construction to that used in the absorption step, at or near the top of the tower, and passing an inert gas such as air or nitrogen or preferably steam up the tower. The temperature of the solution during the regeneration step may be the same as used in the absorption step, i.e., 25 to about 2000C, and preferably 35 to about 1500C. The absorbing solution, after being cleansed of at least a portion of the acid bodies, may be recycled back to the absorbing tower. Makeup absorbent may be added as needed. Single phase is maintained during desorption by controlling the acid gas, e.g., CO2, level so that it does not fall into the region where two liquid phases form. This, of course, following the practice of the present invention, is facilitated by the use of a highly water soluble amino acid in the mixture. As a typical example, during desorption, the acid gas (e.g., CO2)-rich solution from the high pressure adsorber is sent first to a flash chamber where steam and some CO2 are flashed from solution at low pressure. The amount of CO2 flashed off will, in general, be about 35 to 40% of the net C02 recovered in the flash and stripper. This is increased somewhat, e.g., to 40 to 50%, with the high desorption rate promoter system owing to a closer approach to equilibrium in the flash. Solution from the flash drum is then steam stripped in the packed or plate tower, stripping steam having been generated in the reboiler in the base of the stripper. Pressure in the flash drum and stripper is usually 16 to about 100 psia, preferably 16 to about 30 psia, and the temperature is in the range from about 25 to about 2000C, preferably 35 to about l500C, and more preferably 100 to about l400C. Stripper and flash temperatures will, of course, depend on stripper pressure; thus at about 16 to 25 psia stripper pressures, the temperature will preferably be about 100 to about l400C during desorption. Single phase is maintained during desorption by regulating the amount of acid gas, e.g., CO2, recovered. In the most preferred embodiment of the present invention, the acid gas, e.g., CO2, is removed from a gaseous stream by means of a process which comprises, in sequential steps, (1) contacting the gaseous stream with a solution comprising 10 to about 40 weight percent, preferably 20 to about 30 weight percent, of potassium carbonate, an activator or promoter system comprising 2 to about 20 weight percent, preferably 5 to about 15 weight percent, of the diamino compound as herein defined, and 2 to about 20 weight percent, preferably 5 to about 15 weight percent, more preferably 5 to about 10 weight percent, of the amino acid as herein defined, the balance of said solution being comprised of water, said contacting being conducted at conditions whereby the acid gas is absorbed in said solution, and preferably at a temperature ranging from 25 to about 2000C, more preferably from 35 to about 1500C, and a pressure ranging from 100 to about 1500 psia, and (2) regenerating said solution at conditions whereby said acid gas is desorbed from said solution. By practising the present invention, one can operate the process above: described at conditions whereby the working capacity, which is the difference in moles of acid gas absorbed in the solution at the termination of steps (1) and (2) based on the moles of potassium carbonate originally present, is comparable to that obtained under the same operating conditions for removing acid gases from gaseous streams, wherein sterically hindered diamines or diaminoalcohols with fewer methylene groups between the amino groups are employed with an amino acid cosolvent. In other words, working capacity is defined as follows: C02 in solution C02 in solution at completion of less at completion of absorption desorption Which is: Moles of CO2 Absorbed Moles Residual CO2 Absorbed Initial Moles K2C03 less Initial Moles K2C03 It should be noted that throughout the specification wherein working capacity is referred to, the term may be defined as the difference between C02 loading in solution at absorption conditions (step 1) and the C02 loading in solution at regeneration conditions (step 2) each divided by the initial moles of potassium carbonate. The working capacity is equivalent to the thermodynamic cyclic capacity; that is, the loading is measured at equilibrium conditions. This working capacity may be obtained from the vapor-liquid equilibrium isotherm, that is, from the relation between the CO2 pressure in the gas and the acid gas, e.g., CO2 loading in the solution at equilibrium at a given temperature. To calculate thermodynamic cyclic capacity, the following parameters must usually be specified: (1) acid gas, e.g., CO2, absorption pressure, (2) acid gas, e.g., CO2, regeneration pressure, (3) temperature of absorption, (4) temperature of regeneration, (5) solution composition, that is, weight percent amino acid, weight percent diamino compound and weight percent of the alkaline salt or hydroxide, for example, potassium carbonate, and (6) gas composition. Besides providing working capacities and rates of absorption and desorption which are comparable to those of the sterically hindered diamines and other diaminoalcohols useful for this purpose, the specific class of diamines herein are economical and have increased stability in the presence of C02 gas, and the specific class of diaminoalcohols herein additionally have lower volatility than many sterically hindered diamines. Steam requirements are the major part of the energy cost of operating an acid gas, e.g., CO2, scrubbing unit. Substantial reduction in energy, i.e., operating costs, will be obtained by the use of the process wherein the mixture is utilized. Additional savings from new plant investment reduction and debottlenecking of existing plants may also be obtained by the use of the mixture of the invention. The removal of acid gases such as CO2 from gas mixtures is of major industrial importance, particularly the systems which utilize potassium carbonate activated by the unique activator or promoter system of the present invention. While the sterically hindered amines, as shown in U.S. Patent No. 4,112,050, provide unique benefits in their ability to improve the working capacity in the acid scrubbing process, their efficiency may decrease in alkaline "hot pot" (hot potassium carbonate) scrubbing systems at high temperatures and at low concentrations of the acid gas due to phase separation. Therefore, full advantage of the highly effective sterically hindered amines cannot always be utilized at these operating conditions. The addition of an amino acid, as a cosolvent, as shown in U.S. Patent No. 4,094,957, solves the problem of phase separation and enables a more complete utilization of sterically hindered amines as the alkaline materials activator or promoter. This result was unexpected for the reason that many sterically hindered amino acids (including the sterically hindered amino acid, pipecolinic acid) alone, while soluble in these alkaline systems, are not as effective as activators in acid gas scrubbing processes as the other sterically hindered amino compounds. The specific admixture, as instantly claimed and disclosed, while not employing a sterically hindered diamino compound, provides the same working capacity and/or rates of CO2 adsorption as those previously reported in U.S. Patent No. 4,094,957, particularly the N-cyclohexyl 1,3-propanediamine and pipecolinic acid promoter system. The absorbing solution of the present invention, as described above, will be comprised of a major proportion of the alkaline materials, e.g., alkali metal salts or hydroxides and a minor proportion of the amine activator system. The remainder of the solution will be comprised of water and/or other commonly used additives, such as anti-foaming agents, antioxidants, corrosion inhibitors, etc. Examples of such additives include arsenious anhydride, selenious and tellurous acid, proteins, vanadium oxides, e.g., V203, chromates, e.g., K2Cr207, etc. Representative non-sterically hindered diamines for use in the present invention include N,N-diethyl-1,3propanediamine, N-methyl-N-butyl-1,3-propanediamine, N,N-dibutyl-1,3-propanediamine, N-methyl-N-cyclohexyl-l,3- propanediamine, N-methyl-N-cyclohexyl ethylenediamine, N-3-aminopropyl-2-pipecoline, N-(2-aminoethyl)-hexamethyleneimine, N-(3-aminopropyl)-hexamethyleneimine, and the like. Representative non-sterically hindered diaminoalcohols for use herein include N-(2-hydroxyetbyl)-N- (n-propyl)-1,4-butanediamine, N-(2-hydroxyethyl)-N (isopentyl)-l,4-butanediamine, N,N-di (2-hydroxyethyl)1,4-butanediamine, N-(2-hydroxypropyl)-N-methyl-1,4butanediamine, and the like. Representative amino acids applicable herein include: N,N-diethyl glycine, N,N-dimethyl glycine, pipecolinic acid, N-secondary butyl glycine, N-2-amyl glycine, N-isopropyl glycine, N-isopropyl alanine, Nsecondary butyl-alpha-alanine, 2-amino-2-methyl butyric acid, and 2-amino-2-methyl valeric acid. Particularly preferred for use herein are pipecolinic acid and Nsecondary butyl glycine. 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. Examples 1-6 illustrate use of diamines and Examples 7-8 illustrate use of diaminoalcohols. Example 1 The reaction apparatus consists of an absorber and desorber as shown in Figure 1. The absorber is a vessel having a capacity of 2.5 liters and a diameter of 10 cm, equipped with a heating jacket and a stirrer. Pump P1 removes liquid from the bottom of the reactor and feeds it back to above the liquid level through a stainless-steel sparger S1. Vertical baffles further increase the contact between liquid and gas. Thermocouple T permits the reading of the temperature of the liquid. The top of the reflux condenser C is connected to a U-shaped, openended manometer M. The apparatus can be evacuated by means of pump P2 through tap T1. Nitrogen and CO2 can be fed to the bottom of the cell through sparger S2, using respectively taps T2 or T3. CO2, coming from a cylinder, goes first through the two 12-1 flasks F1 and F2, acting as ballasts, then through a 3-1 wet test-meter WTM, then through bubbler B1, where it is saturated with water. Hg-bubbler B2 insures that no air is sucked into flask F2. Constrictions such as narrow tubings and taps have been carefully avoided in the CO2 path. Tap T3, which is the only one inserted in such a path, has a key with large holes (8mum). The desorber is a 1-liter reactor, equipped with teflon blade stirrer, gas spargers S1 and S2, reflux condenser C and thermocouple T. The following reagents were put into a 2-liter Erlenmeyer flask: 55g of N-(3-aminopropyl)-2-pipecoline 22.5g of pipecolinic acid 225g of K2CO3 447.5g of water When all solids had dissolved, the mixture was put into the absorber and brought to 800C, the stirrer being regulated at 1200 rpm. The apparatus was closed and evacuated until the liquid began to boil. The pump for the liquid was regulated so as to circulate about four liters of liquid per minute. At this near-boiling point, C02 gas was admitted into the absorber. In total, 38.7 liters of CO2 were absorbed, correcting for the amount used to fill the vapor space. The rich solution was transferred to the desorber and boiled at 1050C for one hour in a nitrogen flow, with exhaust E open and taps T2 and T3 closed, during which time 30 liters of CO2 were desorbed. Only one liquid phase was present. The regenerated solution so obtained was transferred back to the absorber and cooled to 800C. The apparatus was closed and evacuated until the liquid began to boil. At this point CO2 was admitted. A total of 31.5 liters of CO2 was reabsorbed in 9 minutes, of which 11 liters were absorbed in the first minute. Corrected for the amount of CO2 used to fill the vapor space, the volume of CO2 reabsorbed was 29.5 liters. When the experiment was repeated, replacing the N-(3-aminopropyl)-2-pipecoline and pipecolinic acid with 37.5g of diethanolamine, only 22 liters of CO2 were reabsorbed, and corrected for the CO2 volume used to fill the vapor space, 20 liters were reabsorbed, of which only 4 liters were absorbed in the first minute. Example 2 The reaction apparatus used in this example is a 1-liter autoclave, equipped with Herculite (trademark) windows to enable observation of the contents. A solution of the following ingredients was prepared in an Erlenmeyer flask: 44.59 of N-(3-aminopropyl)-2-pipecoline 18.2g of pipecolinic acid 1809 of K2CO3 357.39 of water A sufficient amount of solid CO2 was then added to the solution to bring the mixture to one phase. The solution was then charged into the autoclave and heated to 1210C. A mixture containing 0.2% CO2 and 99.8% helium gas was slowly blown through the solution at a pressure of 50 psig. The operation was continued until the outgoing gas had the same composition as the entering gas, i.e., 0.2% CO2, as determined by gas chromatography, indicating that equilibrium was reached. Only one phase was present, and the CO2 content was analyzed at 10.9%. Pure CO2 gas was then blown through the solution at a total pressure of 300 psig until the outgoing gas had the same composition as the entering gas. The solution was clear with no precipitate present, and the CO2 content was 18.8%. When the experiment was repeated, replacing the N-(3-aminopropyl)-2-pipecoline and the pipecolinic acid with 5% of diethanolamine, the CO2 content of the liquid varied only from 10.5% to 16.8%. Thus, the diamine herein exhibits not only a rate effect but also an equilibrium effect. Example 3 The following reagents were put into a 2-liter Erlenmeyer flask: 50 g of N- (2-aminoethyl) -hexamethyleneimine 22.5 g of pipecolinic acid 225 g of K2CO3 452.5 g of H2O When all solids had dissolved, the mixture was put into the absorber and an absorption-desorption-reabsorption cycle was carried out as described in Example 1. 37 liters of CO2 were absorbed; 26.4 liters of CO2 were desorbed; and 29.5 liters of CO2 were reabsorbed, of which 8 liters were reabsorbed in the first minute. Example 4 The following reagents were charged into a 2-liter Erlenmeyer flask: 60 g of N-methyl-N-cyclohexyl-1,3-propanediamine 22.5 g of pipecolinic acid 225 g of K2CO3 442.5 g of H2O When all solids had dissolved, the mixture was put into the absorber and an absorption-desorptionreabsorption cycle was carried out as described in Example 1. 36.2 liters of CO2 were absorbed; 27.5 liters of CO2 were desorbed; and 32.8 liters of CO2 were reabsorbed, of which 10 liters were reabsorbed within the first minute. Example 5 The following reagents were charged into a 2-liter Erlenmeyer flask: 55 g of N-methyl-N-cyclohexyl ethylenediamine 22.5 g of pipecolinic acid 225 g of K2CO3 447.5 g of H2O When all solids had dissolved, the mixture was put into the absorber and an absorption-desorptionreabsorption cycle was carried out as described in Example 1. 38 liters of CO2 were absorbed; 28.7 liters of CO2 were desorbed; and 32 liters of CO2 were reabsorbed, of which 10 liters were absorbed in the first minute. Example 6 This example illustrates the stability of the activator system of this invention as compared with the stability of an activator system containing N-cyclohexyl propanediamine, the preferred sterically hindered diamine of U.S. Pat. No. 4,094,957. A stock solution was prepared by mixing 7.40 g of N-(3-aminopropyl)-2-pipecoline, 6.0 g of pipecolinic acid, 2.04 g of potassium bisulfide and 53.2 g of deionized water. The resulting solution had a density of 1.034 g/ml. Twelve identical 10 cc stainless steel ampoules were each charged with 3 cc of the stock solution above described and 1.835 g of potassium bicarbonate. The ampoules were then flushed with nitrogen gas, sealed, and immersed in a constant temperature bath set at 160 + 0.20C, whereupon each ampoule was shaken vigorously for rapid and even temperature equilibration. At pre-set times the ampoules were withdrawn, quenched in cold water and opened. A 3 cc aliquot of isopropanol solution containing a known concentration of an internal standard was added to the opened ampoule together with 2 g of potassium carbonate. The resulting mixture was shaken and stirred to induce complete extraction of the diamine into the isopropanol phase. Gas chromatographic analysis of the isopropanol layer revealed that the rate of degradation of the N-(3-aminopropyl)-2-pipecoline was about 16 times slower than the rate of degradation of N-cyclohexyl propanediamine under the same conditions. Example 7 The following reagents were put into a 2-liter Erlenmeyer flask: 0.35 mole of the diamino compound indicated in Table 1 0.17 mole of pipecolinic acid 225g of K2C03 water to make 750g total solution When all solids had dissolved, the mixture was put into the absorber as described in Example 1 and brought to 800C. The apparatus was closed and evacuated until the liquid began to boil. At this point C02 gas was admitted. At the end of the absorption the rich solution was transferred to the desorber as described in Example 1 and boiled for one hour to desorb the C02 gas. The regenerated solution so obtained was transferred back to the absorber and cooled to 800C. The apparatus was closed and evacuated until the liquid began to boil. At this point C02 gas was admitted. The amount of time taken for the solution to reabsorb 10, 15 and 20 1 of C02 gas was measured, as well as the total amount of C02 gas reabsorbed in the process, designated as capacity to reabsorb. The rich solution containing K2C03, diamino compound and amino acid was regenerated by boiling for an hour, and then was used for a phase-behavior study. About 600 g of regenerated solution were charged into a 1-liter autoclave equipped with Herculite (trademark) window, reflux condenser and inlet and outlet for gases. The autoclave was brought to 121 C while blowing a mixture containing 0.2% C02 gas and 99.8% He gas at about 0.2 liters/minute. When the outgoing gas had the same composition as the entering gas, equilibrium was reached. Only one phase was present in each case. When the experiment was repeated, replacing pipecolinic acid with water, two liquid phases were present at equilibrium. From the results of these tests, shown in Table I, it can be seen that the rates of absorption and the solubilities of all non-sterically hindered diaminoalcohols tested were comparable to the absorption rate and solubility of N-cyclohexyl propanediamine (CHPD) (the preferred sterically hindered diamine in U.S. Patent Nos. 4,094,957 and 4,112,050). TABLE I Time (min:sec) to absorb Capacity (liters indicated volume of CO2 Lean Diamino -Compound* of CO2 reabsorbed) 10 1 15 1 20 1 Solubility N-cyclohexyl propanediamine** 30.0 0:53 1:30 2:21 one phase N-(n-propyl)-N-(2-hydroxyethyl) 1,3 propanediamine** 31.6 0:51 1:25 2:08 one phase N-(n-buthyl)-N-(2-hydroxyethyl) 1,3-propanediamine** 32.7 0:56 1:35 2.19 one phase N-(n-propyl)-N-(2-hydroxyethyl) 1,4-butanediamine 31.8 0:50 1:30 2:30 one phase * In combination with pipecolinic acid ** Controls Example 8 The following experiments were carried out to ascertain the stability of a diaminoalcohol herein under accelerated-simulated acid gas treating conditions. Five standard lean solutions were prepared with the following ingredients: 7.4% by weight of the diamino compound indicated in Table II 3.0% by weight of pipecolinic acid 26.1% by weight of KHC03* 3.9% by weight of K2S** 59.6% by weight of water * represents 87% replacement of 30% K2C03 in solution with KHC03 to simulate presence of C02 gas. ** represents 13% replacement of 30% K2C03 in solution with K2S to simulate presence of H2S gas. A total of 5.4 g of each of these solutions was charged separately into five 10-ml, stainless-steel ampoules, which were each flushed with nitrogen gas and sealed. All of the ampoules were then immersed simultaneously into an oil bath at 1400C and monitored each day by means of gas chromatographic analysis for the amount of original diamino compound remaining in solution. Higher amounts of diamino compound indicate less conversion to by-products and thus greater stability as well as non-volatility at temperatures of l400C. The results are given in Table II. TBLt II % of Original Diamino Di amino Compound* Days at 1400C Compound Remaining CHPD* 7 < 10 N-(n-propyl)-N-(2hydroxyethyl)-l,3- 7 < 8 propanediamine** N- (n-propyl)-N- (2- 2 66 hydroxypropyl)-1,3- 5 44 propanediamine** 12 16 N-(n-propyl)-N-(3- 2 20 hydroxypropyl) -1,3- propanediamine** 5 9 N-(n-propyl)-N-(2- 2 80 hydroxyethyl)-1,4- 5 73 butanediaine 12 59 *In combination with pipecolinic acid **Controls It can be seen that the diaminoalcohol of this invention, represented by the fifth diamino compound in this table, exhibited superior stability as compared not only with CHPD, but also with homologous diaminoalcohols. In summary, the present invention is seen to provide a class of non-sterically hindered diamino compounds which perform effectively in acid gas scrubbing processes and are relatively stable to the acid gases present in the system.

Claims: CLAIMS 1. A process for the removal of C02 from a gaseous stream containing C02 wherein in an absorption step, C02 is absorbed from said gaseous stream with an aqueous absorbing solution comprising (a) a basic alkali metal salt or hydroxide selected from ' alkali metal bicarbonates, carbonates, hydroxides, borates, phosphates and their mixtures, and (b) an activator or promoter system for said basic alkali metal salt or hydroxide comprising (i) at least one non-sterically hindered diamino compound which is defined as a diamine containing both a primary and a tertiary amino moiety wherein the primary amino moiety is attached to a primary carbon atom or as a diaminoalcohol containing a tertiary amino moiety separated by four methylene groups from a primary amino moiety and containing at least one hydroxyl group, and (ii) an amino acid which has the capability to increase the solubility of said diamino compounds in alkaline aqueous conditions at elevated temperatures, and (2) in a desorption and regeneration step, at least a portion of the absorbed C02 is desorbed from said absorbing solution. 2. A process according to claim 1 wherein the aqueous solution contains 10 to about 40% by weight of said basic alkali metal salt or hydroxide, 2 to about 20% by weight of said diamino compound, and 2 tb about 20% by weight of said amino acid. 3. A process according to claim 1 or 2 wherein said amino acid has 4 to 8 carbon atoms per molecule and is free of any hydroxyl groups and is either a tertiary amino acid wherein the amino moiety is a tertiary amino moiety or a sterically hindered amino acid containing at least one secondary amino moiety attached to either a secondary or tertiary carbon atom or a primary amino moiety attached to a tertiary carbon atom. A A process according to any one of claim 1-3 wherein said diamino compound is represented by the following general formulae: H2N(CH2)nNRR' or H2N(CH2)nN & H2)m wherein R and R' independently represent a C1 - C6 alkyl or a C6 - Cg cycloalkyl group, n is an integer of at least 2, and m is an integer of at least 4. 5 A process according to any one of claim 1-3 wherein said diamino compound is represented by the following general formula: H2N ----- (CH2)4 ------- NRR' wherein R and R' each independently represent a C1 - C6 alkyl group and either R or R' or both R and R' have a trrmin;rpendent hydroxyl group. 6. A process according to any one of claim 1-3 wherein said amino acid is pipecolinic acid or N-secondary butyl glycine, said basic alkali metal salt or hydroxide is potassium carbonate, and said diamino compound is N-(3aminopropyl)-2-pipecoline, N-(2-aminoethyl)-hexarnethyl- eneimine, N-ethyl-N-cyclohexyl-1,3-propanediamine, N-methyl-N-cyclohexyl ethylenediamine or N-(2-hydroxyethyl)-N-(n-propyl)-1,4-butanediamine. 7 A process of any one of claims 1-6 wherein the temperature of the absorbing solution during the absorption step is in the range of from about 250 to about 2000C, the pressure in the absorber ranges from about 5 to about 2000 psia, and the partial pressure of the acid components in the feed stream ranges from about 0.1 to about 500 psia and wherein the temperature of the absorbing solution during the regeneration step is in the range from about 250C to about 2000C and at pressures ranging from about 16 to 100 psia. 8. A process according to any one of claim 1-7 wherein the absorbing solution additionally includes one or nQore anti foaming agents, antioxidants or corrosion inhibitors. 9. An aqueous acid gas scrubbing composition comprising (a) 10 to about 40% by weight of an alkali metal salt or hydroxide, (b) 2 to about 20% by weight of a non-sterically hindered diamino compound which is defined as a diamine containing both a primary and a tertiary amino moiety wherein the primary amino moiety is attached to a primary carbon atom or as a diaminoalcohol containing a tertiary amino moiety separated by four methylene groups from a primary amino moiety and containing at least one hydroxyl group, (c) 2 to about 20% by weight of an amino acid which has the capability to increase the solubility of said diamino compounds in alkaline aqueous conditions at elevated temperatures, and (d) the balance, water. 10. An aqueous acid gas scrubbing composition according to claim 9 containing (a) 20 to 30% by weight of potassium carbonate, (b) 5 to about 15% by weight of N-(3-aminopropyl)-2-pipecoline or N-(2-hydroxyethyl)-N-(n-propyl)1,4-butanediamine, (c) S to 10% by weight of pipecolinic acid, and (d) the balance, water.

Inventors: KIM, CHANG JUNG, MELCHIOR, MICHAEL THOMAS, SARTORI, GUIDO, SAVAGE, DAVID WILLIAM, THALER, WARREN ALAN
Applicants: EXXON RESEARCH AND ENGINEERING COMPANY
Application year: 1982
Main classification: B01D53
IPC codes: B01D53