NO172179B - DIAMINOETS FOR USE TO REMOVE H2S FROM REGULARLY GASFUL MIXTURES, AND THEIR PREPARATION - Google Patents

Description

The present invention relates to diamino ethers and more specifically di-secondary and tertiary amino ethers for the removal of H2S from gas mixtures.

The treatment of acid gas mixtures containing CO2 and H2S by means of aqueous amine solutions in an absorption tower typically results in the simultaneous removal of significant amounts of both CO2 and ItøS. In such a process, which is generally called "aqueous amine process", relatively concentrated amine solutions are used. A later improvement of this process entails the use of sterically hindered amines to achieve somewhat close to total removal of acid gases such as CO2 and E2S. This type of process can be used where the partial pressures for CO2 and related gases are low. Another process often used for special applications where the partial pressure of CO2 is extremely high and/or many acid gases are present, such as E2S, COS, CH3SH and CS2, involves the use of an amine in combination with a physical absorbent, usually called a "non-aqueous solvent process". An improvement to this process involves the use of sterically hindered amines and organic solvents as physical absorbents.

However, it is often desirable to treat acidic gas mixtures containing both CO2 and EtøS in order to selectively remove EtøS from the mixture and at the same time minimize the removal of CO2. Selective removal of H2S results in a relatively high H2S:C02 ratio in the separated sour gas, which facilitates the conversion of ItøS to elemental sulfur using the Claus process.

The typical reactions of aqueous secondary and tertiary amines with CO2 and E2 can be represented as follows:

where R is an organic residue which may be the same or different and be substituted with a hydroxyl group. The above-mentioned reactions are reversible and the partial pressures for both COg and H2S are thus important with a view to determining the rate at which the above-mentioned reactions progress.

While selective ^S removal can be applied to a number of gas treatment operations including the treatment of hydrocarbon gases from shale pyrolysis, refinery gas and low HgSrCC^ ratio natural gas, it is particularly desirable in the treatment of gases in which the partial pressure of ItøS is relatively low compared to that of CO2 because the capacity for an amine with a view to absorbing HgS from the latter type of gases is very low. Examples of gases with relatively low partial pressures for H2S include synthesis gases produced by coal gasification, off-gases from sulfur plants and fuel gases with a low Joule content and which occur in refineries where heavy residual oils are thermally converted to low molecular weight liquids and gases.

Solutions of primary and secondary amines such as monoethanolamine (MEA), diethanolamine (DEA), dipropanolamine (DPA) and hydroxyethoxyethylamine (DGA) absorb both H2S and COg gas. Diisopropanolamine (DIPA) is relatively unique among secondary amino alcohols in that it has been used industrially, alone or with a physical solvent such as sulfolane, for the selective removal of H 2 S from gases containing H 2 S and CO 2 .

The tertiary amine-methyldiethanolamine (MDEA) has a high degree of selectivity against ItøS absorption in relation to CO2, but recently it has been discovered that aqueous solutions of dialkylmonoalkanolamines and especially diethylmonoethanolamine (DEAE) have a higher selectivity and capacity for H2S- removal at higher loading levels than MDEA solutions.

It has now been discovered that absorbent solutions of a certain type of amine compounds defined as diamino ethers have a high selectivity for EtøS compared to CO2. These diaminoethers surprisingly retain their high selectivity at high EtøS and CC>2 loadings.

When it comes to a method for removing H2S from normally gaseous mixtures, possibly such mixtures which also contain CO2, reference should be made to NO-PS 164,338.

In a preferred embodiment of the method mentioned in the patent, selective absorption of ItøS from a usually gaseous stream containing CO2 is carried out by bringing the stream into contact with a solution of the diaminoether as described above under conditions where H2S is selectively absorbed from the stream, the diaminoether in addition has a pKa value at 20° C of more than 8.6. The absorbent solution may additionally contain water, a physical absorbent, preferably sulfolane, or a mixture thereof.

In an even more preferred embodiment, after ItøS has been selectively absorbed from the stream, the absorbing solution containing H2S is at least partially regenerated, after which the regenerated solution is returned for selective absorption of H2S upon new contact with the stream. Preferably, the regeneration step is carried out by heating and stripping the solution of absorbed H 2 S and preferably by heating and stripping the solution with steam.

Accordingly, the present invention relates to a diamino ether which is characterized by the general formula:

there

- R<1>, R<2>, R<3> and R<4> are each independently selected from hydrogen and

C1_4 alkyl,

1 and m are positive, whole numbers independently chosen from

and by 2 up to and including 6; and

- n is a positive integer selected from and including 1 to 10;

- X<1> and X<2> are each independently selected from:

there

p is an integer, positive number in the range from 2 to 5; and

R<5 > is selected from primary C 1-3 alkyl groups, each having 1 to 3 carbon atoms, or secondary or tertiary alkyl groups,

provided that when the carbon atom of R<5> directly bonded to the nitrogen atom is primary, both R<1> and R<2> are alkyl groups, and when the carbon atom of R<5> directly bonded to the nitrogen atom is secondary, is at least one of R<1> and R<2> an alkyl group.

A di-secondary amino ether as mentioned above is prepared by a process which comprises the reaction of primary amine with a di-(halo alkoxy)alkane or a bis-sulfonate ester of a glycolic ether at elevated temperature, a di-secondary and tert-amino ether as described above is prepared by a process comprising: (a) contacting a heterocyclic compound having 4 to 9 ring atoms with a haloalkoxyalkanol or a haloalkoxyalkanol at elevated temperature; (b) reacting the product of step (a) with a thionyl halide; and (c) reacting the product of step (b) with a primary

alkylamine at elevated temperature.

The invention shall be described in more detail with reference to the accompanying drawings in which: Figure 1 is a flow chart showing an absorption regeneration unit for the selective removal of H2S from gas streams containing H2S and CO2; Figure 2 is a flow diagram showing an experimental absorber unit for use in rapidly determining the selectivity of the diamino ether for the selective removal of H2S from gas streams containing H2S and CO2; Figure 3 graphically shows the selectivity for E2S against ItøS and CO2 loading for 1,2-bis-(pyrrolidinylethoxy)ethane (BIS-1) and 1,2-bis(piperidinylethoxy)ethane (BIS-PIP), compared to methyldiethanolamine ( MDEA) as control; Figure 4 graphically shows the selectivity for H2S against H2S and CO2 loading for bis-(N-pyrrolidinylethyl)ether (BIS-O), 1,2-bis(pyrrolidinyloxyetoxy)ethane (BIS-2) and 1,2-bis- (3-pyrrolidinyl-n-propoxy)ethane (BIS-P); Figure 5 graphically shows the selectivity for H2S against H2S and the CO2 load for l-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy)ethane (PETBEE) compared to 5-butylaminoethoxyethanol (TBEE) as a comparison and methyldiethanolamine (MDEA) as a control; Figure 6 graphically shows the selectivity for E2S against EtøS and CO2 load for 1,2-bis-(tert-butylaminoethoxy)ethane (BIS-TB) compared to tert-butylaminoethoxyethanol

(TBEE), 1,2-bis-(isopropylaminoethoxy)ethane (BIS-IP)

and methyldiethanolamine (MDEA) as a control.

The diaminoethers generally useful in the described process include mono- or polyether compounds which may be di-tertiary amino ethers, di-secondary amino ethers or di-mixed tertiary and secondary amino ethers.

The tertiary amine groups in the diamino ethers can be acyclic or in the form of a nitrogen heterocycle. If the amine moiety is heterocyclic, it may contain one or more rings, each typically having 4 to 9 ring atoms and preferably 4 to 7 ring atoms, wherein one of the ring atoms is nitrogen. The ring or rings may be substituted or unsubstituted. Furthermore, the rings can be azabicyclic where two rings are fused so that they share at least one side and one of the ring atoms is nitrogen. The nitrogen atom that forms the tertiary amino moiety in such a compound is located in the bicyclic framework in a bridgehead or non-bridgehead ring position. The oxygen atom in the ether functionality may be directly bound to the ring or be separated from the ring by a hydrocarbon chain, arranged in a linear or branched manner, which is bound to the ring via a ring nitrogen or a ring carbon atom.

The secondary amine groups in the diamino ethers are severely sterically hindered secondary amine groups. The term "severely sterically hindered" means that the nitrogen atom in the amine is bound to one or more bulky carbon groups. Characteristically, the secondary amine groups will have a degree of steric hindrance so that the cumulative ~Es value (Taft's steric hindrance constant) is greater than approx. 1.75, calculated from the values given for primary amines in Table V in an article by D.F. DeTar, "Journal of Organic Chemistry", 45, 5174 (1980).

Typical di-tertiary amino ethers and di-mixed tertiary and secondary amino ethers that can be used in this method can be represented by one of the following general formulas:

or or

where R 1 , R 2 , R 9 and R 9 are each independently alkyl, hydroxyalkyl, cycloalkyl or hydroxycycloalkyl residues, R and R' are each independently hydroxyl, alkyl, hydroxyalkyl, cycloalkyl or hydroxycycloalkyl residues which are any substituents on the nitrogen heterocyclic ring, R3, R4, R5, R^, R7 and Rg are independently each hydrogen or a C^^-alkyl or C1-4-hydroxyalkyl residue, m, n and p are positive integers each independently within the range of 2 to 4, o is either 0 or a positive integer from 1 to 10 and q and r, which represent the number of carbon atoms in the heterocyclic ring, are each independently positive integers in the range 3 to 8. If one of

the amino groups are a severely sterically hindered secondary amine, R^ or R 10 , but not attached, may be hydrogen, but only if R 2 or R 8 (whichever is relevant) is an alkyl or hydroxyalkyl residue of 2 to 8 carbon atoms or a cycloalkyl - or hydroxycycloalkyl radical of 3 to 8 carbon atoms, provided that if the carbon atom of R2 or Rg directly bonded to the nitrogen atom is secondary, at least one of R3 or R4, or R7 or Rg (as) is an alkyl or hydroxyalkyl radical, and if the carbon atom in R2 or Rg which is directly bonded to the nitrogen atom is primary, then both R3 and R4 or both R7 and Rg are (because) alkyl or hydroxyalkyl residues. In the latter case, R 2 is preferably a tert-butyl, cycloalkyl, 1-methyl-1-ethyl-propyl or tert-amyl radical, most preferably a tert-butyl radical.

Representative such di-tertiary and di-mixed amino ethers that can be used for H2S removal include, for example, 1,2-bis-(N,N-dimethylaminoethoxy)ethane, bis-(N-pyrrolidinylethyl)ether, N-pyrrolidinylethoxyethyl-N, N-diethylamine, 1,2-bis-(pyrrolidinylethoxy)ethane, 1,2-bis-(pyrrolidinylethoxy)ethane, 1,2-bis-(3-pyrrolidinyl-n-propoxy)ethane, 1,2-bis-( piperidinylethoxy)ethane, 1,3-bis-(piperidinyl-n-propoxy)propane, l-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy)ethane, 1,2-bis-(azepanylethoxy)ethane, l-( pyrrolidinylethoxy)-2-(piperidinyl-ethoxy)ethane, l-(pyrrolidinylethoxy)-2-[2-(t-butylamino)-propoxy]ethane, l-(pyrrolidinylethoxy)-2-(2-isopropylamino)-propoxyethane, l -(pyrrolidinylethoxy)-2-(1-methyl-1-ethylpropylaminoethoxy)ethane, 1-(pyrrolidinylethoxy)-2-(t-amylaminoethoxy)ethane and the like.

Preferred di-tert-amino ethers are represented by the following general formula:

where R and R' are each independently alkyl or cycloalkyl residues which are substituents on the nitrogen heterocyclic ring, q and r are each independently positive whole numbers from 3 to 5, m and p are positive whole numbers each independently within the range 2 to 3 and o is either 0 or a positive integer from 1 to 4. Of this group, the most preferred di-tertaminoethers are one or more compounds selected from bis-(N-pyrrolidinylethyl)ether, 1,2-bis-(pyrrolidinyloxyethoxy)ethane, 1 ,2-bis-(pyrrolidinylethoxy)ethane, 1,2-bis-(piperidinylethoxy)ethane, 1,-bis-(3-pyrrolidinyl-n-propoxy)ethane and 1-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy) ethane.

The new class of di-secondary amino ethers and di-mixed sec- and tert-amino ethers according to the invention which are usable for HgS removal can, as mentioned above, be represented by the general formula:

where the substituents have the above-mentioned meaning.

The new di-secondary amino ethers according to the invention are preferably represented by the following general formula:

wherein R-1 and Rg are each independently selected from sec-alkyl or sec-hydroxyalkyl radicals having 3 to 8 carbon atoms, or tert-alkyl or tert-hydroxyalkyl radicals having 4 to 8 carbon atoms, Rg and Rf, each independently selected from hydrogen and C1_4~ alkyl radicals, provided that when R 1 and R 8 are secondary alkyl radicals, both R 2 and R 2 are C 1-4 alkyl radicals, and o is either 0 or a positive integer from 1 to 4. More particularly, R 2 and R 3 are tert-butyl , tert-amyl or cycloalkyl residues, for

for example cyclopentyl, cyclohexyl or isopropyl residues. Most preferably, R 1 and R 8 are both tertiary butyl residues and R 2 and R fc are hydrogen. When R 1 and R 2 are sec-alkyl radicals, for example isopropyl, it is preferred that each of R 2 and R 2 is a methyl radical. The symbol o is preferably 0 or an integer 1 or 2.

The new di-sec-amino ethers according to the invention can be prepared by reacting a suitable amine, for example R^-NEg and Rg-NHg, with a di-(halogeno-alkoxy)alkane or a bis-sulfonate ester of a glycol ether at elevated temperatures and under conditions so that the halogen acid or sulphonic acid is eliminated. For example, 1,2-bis-(t-butylaminoethoxy)ethane can be prepared by reacting t-butylamine with 1,2-(bis-chloroethoxy)ethane in a solvent such as ethylene glycol monomethyl ether under reflux conditions. The product can be readily recovered by treating the hot solution with an excess of an alkali hydroxide followed by filtration and distillation of the product.

The preferred class of di-mixed sec- and tert-amino ethers can be represented by the formula:

where R is an alkyl or cycloalkyl residue which is a substituent on the nitrogen heterocycle, R^ is a branched alkyl residue with 3 to 8 carbon atoms of which the carbon atom directly bonded to the nitrogen atom is tertiary, q is an integer from 3 to 5, m and p are positive integers each independently in the range 2 to 3 and o is either 0 or a positive integer from 1 to 4.

These new di-mixed-amino ethers can be prepared by a non-catalytic process comprising (1) contacting a heterocycle of 4 to 9 ring atoms with a haloalkoxyalkanol or a haloalkoxyalkanol at elevated temperatures, preferably in the presence of a solvent, (2) reaction of the resulting obtained N-(hydroxyalkoxyalkyl)heterocycle or N-(hydroxyalkoxyalkyl)heterocycle from step (1) with a thionyl halide such as thionyl chloride, preferably in a solvent, to obtain an N-(haloalkoxyalkyl)heterocycle or N-(haloalkoxy -alkoxyalkyl)heterocycle and (3) reacting the isolated product of step (2) with a primary alkylamine at elevated temperatures, preferably in the presence of a solvent, to obtain the di-mixed amino ether.

Typical primary alkylamines which can be used in the above-described manufacturing process are isopropylamine, tert-butylamine and tert-amylamine. Typical haloalkoxyalkanols are, for example, 2-chloroethoxyethoxyethanol. Suitable heterocycles are azepane, pyrrolidine, piperidine and the like. Typical solvents for steps (1) and (3) are lower alkanols and ethers such as methanol, ethanol, propanol, ethylene glycol monomethyl ether, diethyl ether, tetrahydrofuran and the like. Preferably, the solvent is a polar solvent and most preferably it is ethanol or ethylene glycol monomethyl ether. The solvents generally used for step (2) are non-polar solvents such as toluene.

Steps (1) and (3) in the manufacturing process stated above are carried out at least at temperatures in the range of 50 to approx. 250°C, and most preferably from 100 to approx. 200°C. Step (3) is preferably carried out in an autoclave. During step (2), the N-(hydroxyalkyloxyalkyl)heterocycle is generally added as a solution dropwise to the thionyl halide in solution without the commonly used elevated temperatures.

Representative new diaminoethers from all categories are, for example, bis-(tert-butylaminoethyl)ether, 1,2-bis-(tert-butylaminoethoxy)ethane, 1,2-bis-(tert-butylaminoethoxyethoxy)-ethane, bis-[2- (isopropylamino)propyl]ether, 1,2-[2-(isopropyl-amino)propoxy]ethane, 1-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy)ethane, 1-(pyrrolidinylethoxy)-2-[2-( t-butylamino)propoxy]ethane, 1-(pyrrolidinylethoxy)-2-[2-(2-isopropylamino)propoxy]ethane, . l-(pyrrolidinylethoxy)-2-(1-methyl-l-ethylpropylaminoethoxy)ethane, l-(piperidinyl-n-propoxy)-2-(t-butylaminoethoxy)ethane and l-(azepanylethoxy)-2-(t-butylaminoethoxy) )ethane.

The most preferred new diaminoethers according to the invention from each category are 1,2-bis-(tert-butylaminoethoxy)ethane and 1-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy)ethane.

The diaminoethers used in the selective absorption process as described are further characterized by a pKa value at 20°C of over 8.6, preferably over 9.5 and most preferably the pKa value for the diaminoether lies within the range 9.5 to 10.6 . If the pKa value is less than 8.6, the reaction with HgS will be reduced, while if the pKa value for the diamino ether is much greater than approx. 10.6, an excessive amount of steam will be required to regenerate the solution. In order to thus ensure operating efficiency with minimal loss of diamino ether, the diamino ether can have a relatively low volatility. For example, the boiling point of the amine at 760 mm is characteristically greater than approx. 180°C, preferably greater than 200°C and most preferably greater than 225°C.

The diamino ethers described here can also be characterized by their high solubility in water under conditions for HgS removal and most of the compounds are also generally soluble in polar organic solvent systems which may possibly contain water. The term "absorbent solution" as used here denotes solutions in which diamino ethers are dissolved in a solvent, preferably selected from water or a physical absorbent or a mixture of water and physical absorbent. Solvents that are physical absorbents (as opposed to the diaminoethers that are chemical absorbents) solubilize the diaminoethers and include, for example, aliphatic acid amides, N-alkylated pyrrolidones, sulfones, sulfoxides, glycols and mono- and diethers thereof. The preferred physical absorbents are sulfones and preferably sulfolane.

The absorbing solution can have a concentration of the diamino ether of approx. 0.1 to 6 mol/liter total solution and preferably 1 to 4 mol/liter, primarily depending on the specific diamino ether used and the solvent system used. If the solvent system is a mixture of water and a physical absorbent, the typical effective amount of the physical absorbent used will vary from 0.1 to 5 mol/liter of total solution and preferably from 0.5 to 3 mol/liter, depending mainly on the type of diamino ether used. The dependence of the concentration of the diamino ether on the particular compound used is significant because an increase in the concentration of diamino ether can reduce the basicity of the absorbent solution and thereby adversely affect its selectivity for HgS removal, especially if the diamino ether has a specific water solubility limit that determines the maximum concentration levels within the given range. It is therefore important that the concentration level that is appropriate for each particular diamino ether is maintained to ensure satisfactory results.

The solution can include a number of additives which are characteristically used in selective gas removal, for example anti-foaming agents, antioxidants, corrosion inhibitors and the like. The amount of these additives will characteristically lie within the range in which they are effective, that is to say an effective amount.

Furthermore, the diaminoethers described here can be mixed with other amino compounds, (for example amines other than those used as diaminoethers) as a mixture, preferably with methyldiethanolamine, to form the absorbent solution. The ratio between the respective amino compounds can be varied within wide limits, for example from 1 to 99% by weight of the diamino ethers described here.

Three characteristics of ultimate importance in determining the effectiveness of the diaminoethers for EgS removal are "selectivity", "loading" and "capacity". The term "selectivity" as used in this specification is defined as the following mole ratio fraction:

The higher this fraction, the greater the selectivity for the absorbing solution of EgS in the gas mixture.

The term "load" means the concentration of EgS and COg gases that are physically dissolved and chemically bound in the absorbing solution, expressed in moles of gas per moles of amine. The best diamino ethers are those that show good selectivity up to a relatively high loading level. The diaminoethers as they are used in carrying out the invention can have a "selectivity" of not significantly less than 10 at a "loading" of 0.1 mol, preferably a "selectivity" of not significantly less than 10 at a "loading" of 0, 2 or more moles of EgS and COg per moles of diamino ether.

"Capacity" is defined as the number of moles of EgS in the absorbing solution at the end of absorption minus the number of moles of H2S in the absorbing solution at the end of the desorption step. The increased capacity makes it possible to reduce the amount of amine solution to be circulated and to use less heat or steam for the regeneration.

The diamino ethers described here are typically capable of reducing the EgS level in gas mixtures to a relatively low level, for example less than approx. 200 ppm, and characteristically has a relatively high capacity with regard to H2S, for example over 0.2 mol H2S per moles of amine. The diamino ethers can be characterized as having a "kinetic selectivity" with respect to H 2 S, that is, a faster reaction rate for H 2 S than for CO 2 under the absorption conditions. In addition, they can be characterized as having a higher capacity for H2S at equivalent kinetic selectivity for H2S in relation to CO2. These higher capacities result in the economic advantage of lower steam requirements during regeneration.

The usually gaseous stream described here necessarily contains H2S, usually in gaseous form. (The term "usually" refers to ambient conditions in terms of temperature and pressure.) It may optionally contain other gases such as C02, N2, CH4, CO, H20, COS, HCN, C2H4, NH3 and the like. Such gas mixtures are often found in combustion gases, refinery gases, town gas, natural gas, synthesis gas, water gas, propane, propylene, heavy hydrocarbon gases and so on. The absorbent solution is particularly effective when the gaseous mixture is a gas obtained for example from shale oil retort gas, coal or heavy oil gasification with air/steam or oxygen/steam, thermal conversion of heavy residual oils to low molecular weight liquids and gases, or in residual gases from sulfur plant purification .

The absorption step usually involves contacting the usually gaseous stream with the absorbent solution in any separate contact container. In such processes, the usually gaseous mixture from which H 2 S is to be removed can be brought into intimate contact with the absorbent solution using conventional means such as a tower, for example, pack of rings or sieve plates, or a bubble reactor.

In a typical embodiment of the process where H 2 S is selectively absorbed from a mixture also containing CO 2 , the absorption step is carried out by feeding the usually gaseous mixture to the lower part of the absorption tower while fresh absorbing solution is fed to the upper part of the tower. The gas mixture, substantially freed of EgS, escapes from the upper part of the tower and loaded absorbent solution containing selectively absorbed EgS leaves the tower near the bottom. Preferably, the inlet temperature of the absorbent solution during the absorption step is in the range from 20 to 100° C., and most preferably from 40 to 60° C. The pressure can be varied within wide limits, acceptable pressures are in the range 0.4 to 140.6 kg/ cm2 , preferably between 1.4 and 105.5 kg/cm<2> and most preferably between 1.8 and 70.3 kg/cm<2> in the absorber. The contact takes place under conditions such that EgS is selectively absorbed by the solution.

The absorption conditions and apparatus are designed to minimize the residence time of the liquid in the absorber to reduce COg uptake, while at the same time maintaining sufficient residence times for the gas mixture together with the liquid to be able to absorb a maximum amount of EgS gas. The amount of liquid required for circulation to provide a given degree of EgS removal will depend on the chemical structure and basicity of the diamino ether and on the partial pressure of EgS in the feed gas. Low partial pressure gas mixtures such as those produced in thermal conversion processes will require more liquid under the same absorption conditions than higher partial pressure gases such as shale oil retort gases.

A typical procedure for selective EgS removal involves selective absorption of EgS via countercurrent contact between a gaseous mixture containing EgS and COg with the solution of the diamino ether in a column containing a number of dishes at a low temperature, for example below 45°C, and at a gas velocity of at least approx. 9.1 g/sec. (based on "active" or aerated bowl surface), depending on the operating pressure for the gas, as the bowl column has less than 20 contact bowls, and where, for example, 4 to 16 bowls are typically used. Alternatively, packed layers can be used instead of bowls.

After contact between the usually gaseous mixture and the absorbing solution which becomes saturated or partially saturated with EgS, the solution can be at least partially regenerated so that it can be returned to the absorber. As with the absorption, the regeneration can occur in a single liquid phase. The regeneration or desorption of acid gases from the absorbing solution can be carried out by conventional means such as reducing the pressure over the solution or increasing the temperature to a point where absorbed EgS is driven off, or by passing the solution into a container of the same construction as was used in the absorption step , at the upper part of the container, and passing an inert gas such as air or nitrogen or preferably steam upwards through the container. The temperature of the solution during the regeneration step should lie within the range of 85 to 170°C, and preferably from 80 to 120°C, and the pressure of the solution during the regeneration should lie from 0.04 to 7.0 kg/cm2 , preferably 0.07 to 3 .5 kg/cm2. After it has been cleaned of at least part of the EgS gas, the absorbent solution can be returned to the absorption container. Fresh absorbent liquid can be added as needed.

In the preferred regeneration technique, the EgS-rich solution is sent to the generator where absorbed components are stripped using steam obtained by boiling the solution. The pressure in the flash drum and stripper is usually 0.07 to 3.5 kg/cm 2 , preferably 1.05 to 2.1 kg/cm 2 , and the temperature is typically in the range of 50 to 170°C, preferably 80 to 120°C. The stripping and flash temperatures will of course depend on the pressure, so for example the temperature will be 80 to 120° C during the desorption at a stripping pressure of 1.05 to 2.1 kg/cm2. Heating of the solution to be regenerated can very suitably be carried out entirely by indirect heat exchange with low-pressure steam. However, it is also possible to use direct steam blowing.

In an embodiment for carrying out the entire process described here as shown in Figure 1, the gas mixture to be purified is supplied through pipeline 1 to the lower part of a gas-liquid counter-current contact column 2 where the contact column has a lower part 3 and an upper part 4 The upper and lower parts can be separated from each other by one or more packed layers as desired. The absorbing solution as described above is supplied to the upper part of the column through a pipeline 5. The solution flowing to the bottom of the column meets the gas in countercurrent and preferentially dissolves EgS. Gas that has been freed of most of its EgS exits through a pipeline 6 for final use. The solution, mainly containing EgS and some COg, flows towards the bottom of the column from where it is discharged through pipeline 7. The solution is then pumped via a possible pump 8 through a possible heat exchanger and cooler 9 arranged in the pipeline 7 and which allows the hot solution from the regenerator 12 exchanges its heat with colder solution from absorber column 2 to conserve energy. The solution passes via pipeline 7 to a flash drum 10 equipped with a pipeline, not shown, which aerates out to pipeline 13 and is then supplied via pipeline 11 to the upper part of the regenerator 12 which is equipped with several plates and which causes desorption of HgS and C02 gases carried along. The acidic gas mixture is led through a pipeline 13 to a condenser 14 where cooling and condensation of water and amine solution from the gas is carried out. The gas is then led to a separator 15 where further condensation is carried out. The condensed solution is returned through pipeline 16 to the upper part of the regenerator 12. The gas from the condensation, which contains EgS and some COg, is removed through pipeline 17 for final use (for example for aeration or to an incinerator or an apparatus that converts HgS to sulfur , such as a Claus unit or a Stretford conversion unit.

The solution is freed of most of the gas it contained as it flowed down through the regenerator 12 and exits through conduit 18 at the bottom of the regenerator for transfer to a reboiler 19. This is equipped with an external heat source (e.g. steam blown into through conduit 20 and condensate exiting through a second conduit not shown), a portion of this solution (mainly water) evaporates to drive off additional HgS. HgS and steam which is driven off is returned via pipeline 21 to the lower part of the regenerator 12 and exits through pipeline 13 for supply to the condensation stage of the gas treatment. The solution remaining in the reboiler 19 is drawn off through pipeline 22, cooled in the heat exchanger 9 and supplied by means of a pump 23 (which is not necessary if the pressure is sufficiently high) through pipeline 15 to the absorber column 2.

The diaminoethers according to the invention have been found to be superior to those previously used, especially MDEA and DEAE, expressed both in terms of selectivity and capacity to maintain selectivity over a wide load range. Typically, a gaseous stream to be treated has a HgS:COg molar ratio of 1:10 and it comes from a heavy residual oil thermal reformer or a Lurgi coal gas with a HgS:COg molar ratio of less than 1:10, give an acidic gas with a mole ratio HgS:C0g of approx. 1:1 after treatment by the method according to the invention. The process described here can be used in conjunction with other HgS-selective processes, however, it is preferred to carry out the method according to the invention alone because the diaminoethers are extremely effective in themselves for preferential absorption of HgS.

The invention shall be further illustrated by means of the following examples, which shall not, however, be limiting in any way. All parts and percentages are, unless otherwise expressly stated, by weight. All pKa values are measured at 20°C, unless otherwise stated.

Examples of di-tert-amino ethers

EXAMPLE 1

Preparation of 1. 2-bis-(pyrrolidinylethoxy)ethane (BIS-1)

To a solution of 153 g of pyrrolidine in 950 ml of tetrahydrofuran (THF) was added 217.8 g of triethylene glycol ditosylate in 1400 ml of THF at ambient temperature over the course of 2.5 hours. The reaction was refluxed overnight. The solvent was then removed under reduced pressure and the residue extracted several times with diethyl ether. Evaporation of the ether and distillation of the residue gave an 85% yield of the product as a colorless oil with a boiling point of 123 to 125°C at 0.15 mm.

Analysis for C-^HggNg^1

EXAMPLE 2

Alternative preparation of 1. 2- bis-(pyrrolidinylethoxvletane ( BIS-1)

To a solution of 500 g or 7.05 mol of pyrrolidine in 1600 ml of ethylene glycol monomethyl ether was added 298 g or 1.6 mol of 1,2-bis-(chloroethoxy)ethane in 250 ml of ethylene glycol monomethyl ether. The reaction mixture was refluxed overnight, cooled slightly and reacted with 197 g or 3.52 mol of KOH. After heating for 1 hour, the reaction mixture was cooled, filtered and the solvent was stripped off in a rotary evaporator under reduced pressure. Extraction of the residue with ether and distillation of the ether residue gave 682 g or 83% of the bis-amino ether bp 108 to 110°C at 0.06 mm.

EXAMPLE 3

Preparation of bis-(pyrrolidinylethoxyethyl) ether (BIS-2)

The experimental procedure as described in Example 1 was repeated using pyrrolidine and tetraethylene glycol ditosylate to obtain the desired product which had a boiling point of 150°C at 0.25 mm.

Analysis for C-L5<H>32<N>2O3:

EXAMPLE 4

Preparation of 1. 2-bis-(3-pyrrolidinyl-n-propoxy) ethane

(BIS-P)

To a suspension of 25 g of LiAlH 4 in 500 ml of THF was added 140 g of dimethyl-4,7-dioxadecanedioate in 200 ml of THF in an amount sufficient to maintain reflux. Reflux was continued for a further 5 hours. The cooled reaction mixture was then decomposed in sequences with 25 g of water, 25 g of 15% NaOH and 64 ml of water, filtered and distilled to give 1,2-bis-(3-hydroxy-n-propoxy) in 76# yield )ethane, a glycol ether with a boiling point of 132°C at 0.3 mm.

To 63 g of the above-mentioned glycol ether in 64 ml of dry pyridine, cooled to -10°C, 135.6 g of p-toluenesulfonyl chloride in 200 ml of dry pyridine were added over the course of 0.75 hours. The reaction mixture was kept at -10°C for an additional 2 hours and then poured into 1 liter of ice water. The precipitated product, 1,2-bis-(3-hydroxy-n-propoxy)ethane ditosylate, was filtered, washed with water and dried to give 83% product with melting point 59-60°C.

A total of 30 g of pyrrolidine was added to a hot solution of 39 g of 1,2-bis-(3-hydroxy-n-propoxy)ethane ditosylate in 200 ml of ethylene glycol monomethyl ether and refluxed overnight. 10 g of KOH was added and reflux was continued for 0.5 h. The cooled reaction mixture was filtered and the filtrate concentrated under reduced pressure. The residue was stirred with 300 ml of THF, filtered and distilled. The product was obtained in 85% yield and had a melting point of 130° C. at 0.1 mm.

Analysis for C15<H>32<N>2O2:

EXAMPLE 5

Selective ^ S- f. ironation from a mixture containing H2 S and C02

Figure 2 shows the absorber unit which works according to the half-batch principle, and which is used to assess the selectivity of H2S removal in the amino ethers in the method of the invention. A gas mixture consisting of 10$ CO 2 , 1% H 2 S and 89% N 2 , expressed in volume-#, is passed from a gas cylinder not shown through pipe 30 to a meter 31 which measured the rate at which the gas was fed to the absorber. For all examples this rate was 3.6 l/min. The gas was then led through pipeline 32 to a gas chromatography column, not shown, which continuously calculated the composition of the inlet gas and through pipelines 33 and 34 to the absorber unit 35, which is a cylindrical glass tube with a height of 45 cm and a diameter of 3.1 cm, filled with 100 ml of the absorbent amine solution 36. The gas was passed through the solution at a solution temperature of 40°C and 10 ml samples of the solution were periodically removed from the bottom of the absorber unit through lines 34 and 37 for analysis for H 2 S and CO 2 content. The H2S content in the liquid sample was determined by titration with silver nitrate. The C02 content in the liquid sample was then analyzed by acidifying the sample with an aqueous solution of 10# HC1 and measuring the COg evolved by increasing the weight of NaOH-coated asbestos.

While the solution was periodically withdrawn from the bottom of the absorber, the gas mixture was removed from the top of it via pipe line 38 to a trap 39 which served to wash out the EgS present in the outlet gas. The resulting gas could then optionally be led via pipelines 40 and 41 to final disposal or via pipeline 42 to a gas chromatography column (not shown) for periodic determination of the composition of the outlet gas to investigate possible system leaks. For the purposes of the examples, the content of EgS and COg in the inlet phases was measured and the content of EgS and COg in the liquid phase was determined as described above. These data were used to judge selectivity values for the amine as defined above and which were listed as a function of the loading of absorbing solution of EgS and COg in units of moles of acid gas per moles of diamino ether.

The procedure stated above was used and aqueous solutions of 1.5M 1,2-bis-(pyrrolidinylethoxy)ethane (BIS-1) (pKa = 9.55) and 1,2-bis-(piperidinylethoxy) were used as absorbent solutions. ethane (BIS-PIP) (pKa = 9.61, boiling point = 135"C at 0.09 mm) and an aqueous 3M solution of methyldiethanolamine (MDEA) as a comparison (which represented an amine commonly used for selective EgS- selectivity data for all three amines are shown in Figure 3.

EXAMPLE 6

The procedure in example 5 was repeated and aqueous 1.5 M solutions of bis-(N-pyrroly-dinylethyl) ether (BIS-0) (pKa = 9.75, boiling point = 96°C at 0.37 mm) were used as absorbing solution. , 1,2-bis-(3-pyrrolidinyl-n-propoxy)ethane (BIS-P) (pKa = 10.23, boiling point = 130°C at 0.1 mm) and 1,2-bis-(pyrroli- dinyloxyethoxy)ethane (BIS-2) (kPa = 9.63, boiling point = 150°C at 0.25 mm). A selectivity diagram for all three amines is shown in Figure 4.

Examples of di-mixed amino ether

EXAMPLE 7

Preparation of l-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy)ethane (PETBEE)

A total of 295 g of pyrrolidine and 250 g of 2-chloroethoxyethoxyethanol in 750 ml of ethanol were refluxed for 5 hours. The reaction mixture was then heated with 106 g of KOE and refluxed for an additional 1 hour. Filtration and distillation gave 229 g of N-(hydroxyethoxyethoxyethyl)pyrrolidine with boiling point 145 °C at 3 mm.

A solution of 26.4 g of the above-mentioned amino alcohol in 150 ml of toluene was added dropwise to 16.6 g of thionyl chloride in 200 ml of toluene. One hour after the addition was finished, the reaction mixture had separated into two liquid phases. The lower phase was drawn off, treated with a saturated aqueous sodium carbonate solution and extracted with ether. Distillation of the dried ether solution gave 14 g of N-(chloroethoxyethoxyethyl)-pyrrolidine with a boiling point of 120°C at 3 mm.

A solution of 54.8 g of the thus obtained pyrrolidine derivative and 37.2 g of tert-butylamine in 60 ml of methanol was heated for 3 hours at 150°C in an autoclave. The cooled reaction mixture was removed from the autoclave and treated with 15.6 g of KOE. Filtration and distillation gave 1-(pyrrolidinylethoxy)-2-(tert-butylaminoethoxy)ethane in a yield of 53$ and with a boiling point of 104°C at 0.11 mm.

EXAMPLE 8

Selective Bg S removal from a mixture containing Bo S and CO 0 The procedure from example 5 was repeated and an aqueous 1.5 M solution of 1-(pyrrolidinylethoxy)-2-(tert-butylaminoethoxy)ethane (PETBEE) was used as absorbing solution.

(pKa = 9.25). As a comparison, aqueous 3M solutions of t-butylaminoethoxyethanol (TBEE) and methyl-

diethanolamine (MDEA) using the same conditions, and a selectivity diagram for each amine was listed in Figure 5.

The results given in Figure 5 suggest that the di-mixed amino ether according to the invention is superior to the mono-amino ether alcohol (TBEE) and the tertiary monoamine (MDEA).

Examples of di-sec-amino ethers

EXAMPLE 9

Preparation of 1,2-bis-(t-butylaminoethoxy)ethane (BIS-TB)

A solution of 2.5 mol of t-butylamine and 0.5 mol of 1,2-(bis-chloroethoxy)ethane in 600 ml of ethylene glycol monomethyl ether was refluxed for 3 days. Potassium hydroxide in an amount of 1.2 moles was added portionwise to the hot solution and the reflux was continued for 1 hour. The cooled reaction product was filtered, the solvent stripped off and the residue distilled. The recovered distillate had a boiling point of 104 to 107°C at 0.25 mm and the yield was 75$.

The product, characterized by <1>H-NMR, showed signals at

1.1 (s, 1H), 2.74 (t, 4H), 3.6 (t, 8H).

Analysis for C-L4<H>32<N>2O2:

EXAMPLE 10

Selective Hg S removal from a mixture containing Hg S and COg The procedure from example 5 was repeated and aqueous 1.5M solutions of 1,2-bis-(tert-butylaminoethoxy)ethane (BIS-TB) and 1 ,2-bis-(isopropylaminoethoxy)ethane (BIS-IP) (control) and aqueous 3M solutions of t-butylaminoethoxyethanol (TBEE) (comparison) and methyldiethanolamine (MDE) (control) using the same conditions. Selectivity data for each amine were tabulated as shown in Figure 6.

The results shown in Figure 6 suggest that the di-severe sterically hindered secondary amino ethers according to the invention are far superior to the di-secondary amino ethers which are not severely sterically hindered (BIS-IP), the monoamino-severe sterically hindered amino ether alcohols (TBEE) and the tertiary amine (MDEA).

The data given in figures 3, 5 and 6 also show that the diamino ethers according to the invention have a very high capacity both with regard to HgS and COg, compared to methyldiethanolamine (MDEA), in addition to high HgS selectivities. It will be obvious from an examination of the data given in figures 3, 5 and 6 that if the absorption process is carried out under conditions such that the diaminoethers have a long contact time with the gases to be absorbed, the selectivity for HgS is reduced, but the total capacity for both COg and HgS rather remains high. Therefore, in some cases one may wish to carry out a "non-selective" acid gas absorption process in order to take advantage of the large absorption capacity of the diamino ethers according to the invention. Such "non-selective" processes are particularly useful in scrubbing natural gases containing relatively high levels of HgS and low to zero levels of COg. As such, the diamino ethers according to the invention can replace some or all of the monoethanolamine (MEA) or diethanolamine (DEA) which are usually used for such washing processes.

Although the examples given here illustrate the superior performance of the diaminoethers for selective HgS removal using an absorber unit as indicated in Figure 2, it will also be possible to achieve effective selective HgS removal using the diaminoethers in an absorption regeneration unit as indicated in Figure 1.

In summary, the present invention enables the removal of HgS from gas streams by providing a special class of amino compounds which are characterized as diamino ethers with tertiary and/or secondary amino groups and which have high selectivity towards HgS relative to COg, a selectivity which is maintained at high HgS and COg load levels.

Claims (2)

1. Diamino ether, characterized by the general formula: there R-*-, R<2>, R<3> and R<4> are each independently selected "from hydrogen and C1_4 alkyl, 1 and m are positive, whole numbers independently chosen from and by 2 up to and including 6; and n is a positive integer selected from 1 to 10; X<1> and X<2> are each independently selected "among: there p is an integer, positive number in the range from 2 to 5; and r<5> is selected from primary C^_3 alkyl groups, each having 1 to 3 carbon atoms, or secondary or tertiary alkyl groups, provided that when the carbon atom of R<5> directly bonded to the nitrogen atom is primary, both R<1> and R<2> alkyl groups, and when the carbon atom in R^ which is directly bonded to the nitrogen atom is secondary, at least one of R<1> and R<2> is an alkyl group. 2. Diamino ether according to claim 1, characterized in that it is 1,2-bis-(tert-butylaminoethoxy)ethane or 1-(pyrrolidinylethoxy)-2-(t-butylaminoethoxy)ethane.