The present invention relates to the treatment of streams having mercaptan or mercap- tan-based compounds therein; jnore particularly, it relates to methods for treating such streams by utilizing raitrogen-based promoters as additives to promote the extraction and/or catalytic oxidation of the mercaptan or merσaptan-based compounds therein.

This invention is particularly adapted to a variety of processes for sweetening mercaptan- containing sour hydrocarbon distillate, and is further adapted to the processes for regenerating spent caustic solutions utilized in extracting mercaptan compounds from such sour hydrocarbon distillate.

The art relating to the treatment of mer- captan-containing sour hydrocarbon distillate and the regeneration of spent caustic solutions is well developed and the processes and apparatus therefor are the subject of many patents. For example, U.S. Patent Numbers 2,988,500; 3,371,031; 3,413,215 ^' ; 3,445,380; 3,515,677; 3,574,093; 3,923,645; 3,931,054; 3,972,829; 4,003,827; 4,009,120, 4,018,705; 4,033,860; 4,070,271; 4,087,378; 4,090,954;

4,098,681; 4,107,078; 4,113,604; 4,121,998; 4,121,999; 4,124,531; 4,141,819; 4,206,043; 4,248,694; 4,298,502; 4,364,843; 4,481,106; 4,481,107; 4,490,246; 4,498,977; 4,498,978; and 4,579,121 are representative of catalytic oxidation processes and catalysts for ς treating mercaptan-containing sour hydrocarbon distillate. U. S. Patent Numbers 2,425,414; 2,606,099; 2,740,749; 2,853,432, 2,921,021; 2,937,986; 3,107,213; 4,040,947; 4,081,354; 4,104,155; 4,199,440; and 4,362,614 are representative of extraction and regeneration processes. U. S. Patent Numbers 2,176,806; ια 2,215,359; 2,299,426; 2,662,001; 3,226,092; 3,238,124; 3,351,434; 3,496,996; 3,585,005; 3,758,404; 3,839,487; 3,977,829; 3,989,466; 3,992,156; 4,019,869; 4,039,389; 4,201,626; 4,219,420; 4,364,821; and 4,491,565 are representative of apparatus useful in the practice of various of the aforementioned processes. All of the ^• above-listed patents are hereby incorporated by reference herein for all purposes as if fully set forth.

In general, the sweetening of mercaptan-containing hydrocar¬ bon distillate entails oxidizing the noxious mercaptan compounds to less objectionable disulfides. Commonly used treating proces¬

20 ses provide for contacting the distillates with an oxidising agent, usually air, and a mercaptan oxidation catalyst dispersed in an aqueous caustic solution, usually an alkali metal hydroxide solution. The sour distillate and the catalyst containing aque¬ ous caustic solution provide a liquid-liquid system wherein mer-

25 captans are converted to disulfides in the presence of an

oxidizing agent, usually an oxygen containing gas dissolved in the hydrocarbon being treated.

Sour hydrocarbon distillate containing more difficultly oxidizable mercaptans may also be effectively treated in contact with a mercaptan oxidation catalyst deposited on a high surface area adsorptive support, usually a metal phthalocyanine on an activated charcoal. The distillate is treated in contact with the supported catalyst at oxidation conditions in the presence of an aqueous caustic solution. The oxidizing agent is most often air admixed with the distillate to be treated, and the caustic solution is most often an aqueous alkali metal hydroxide. The caustic solution is charged continuously to the process or inter¬ mittently as required to maintain the catalyst in a caustic- wetted state. Mercaptan-containing hydrocarbon distillate may also be sweetened by contacting the distillate with an aqueous caustic stream whereby the mercaptans are extracted into the caustic in the form of mercaptides. The ercaptide-containing caustic solu¬ tion is then separated from the sweetened distillate and may be recycled until the caustic solution becomes spent, that is, until the caustic solution loses its capacity to extract the mercaptan compounds to such an extent that the process can no longer run efficiently.

Conventionally this spent caustic solution is either discar¬ ded or regenerated for reuse. In general, the regeneration of spent caustic solutions entails oxidizing the mercaptides to

disulfides and extracting or otherwise separating out the result¬ ing disulfides from the caustic solution. Commonly used regene¬ ration processes provide for adding a mercaptan oxidation catalyst to the spent caustic solution then contacting the resulting solution with an oxidizing agent. The mercaptan oxida¬ tion catalyst is usually a metal phthalocyanine and the oxidizing agent is usually an oxygen-containing gas such as air. The cata¬ lyst containing caustic stream and the oxygen-containing gas provide a gas-liquid system wherein mercaptides are converted to disulfides in the presence of the gas, with the resulting disul¬ fides being removed by the settling out thereof. The regenerated caustic stream is then separated from the settled residue for reuse.

The prior art, to a certain extent, recognizes that some nitrogen compounds may be useful in the sweetening and regenera¬ tion processes. For example, U. S. Patent Number 2,508,817 recognizes the use of N-alkyl derivatives of paraphenylene dia¬ mine as catalysts in the oxidation of mercaptans to disul ides. More specifically, the patent teaches a batch process in which a light hydrocarbon oil suitable for motor fuels and having 0.002% or less mercaptan sulfur is contacted with oxygen dissolved in the hydrocarbon oil and from 0.002% to 0.06% by weight of the N- alkyl derivative of paraphenylene diamine also dissolved in the hydrocarbon, to convert the mercaptans to disulfides to sweeten the sour hydrocarbon oil.

U. S. Patent Number 2,565,349 discloses the use of relative¬ ly large amounts of pyridine as a catalyst in the sweetening of sour petroleum distillate. The patent teaches that contacting the sour distillate with a mild oxidizing agent in the presence of 0.1% to 5.0% by volume pyridine and 0.1% to 5.0% by volume alkali solution at temperatures of from 60°F to 200°F will result in the conversion of some mercaptans to disulfides, thereby sweetening the sour distillate.

U. S. Patent Numbers 3,408,287 and 3,409,543 disclose a sweetening process whereby a sour hydrocarbon stream is contacted with an oxidizing agent and a phthalocyanine catalyst in the presence of an alkali .solution containing from 1.0% to 90% by volume of a polar-organic solvent selected from the group con¬ sisting of dialkyl sulfoxides, amino alcohols, amino-hydroxy- alkyl ethers, alkyl amines, alkyl polyamides, alkyl amides and mixtures thereof. U. S. Patent Number 3,409,543 further dis¬ closes regenerating the polar organic solvent containing alkali solution by conventional means.

U. S. Patent Number 3,785,964 discloses a process for sweet¬ ening sour hydrocarbons whereby a sour hydrocarbon stream is contacted with a calcined copper-iron fixed bed catalyst in the presence of 0.0001% to 5% by weight of certain nitrogen com¬ pounds, preferably ammonia or pyridine.

U. S. Patent Number 3,853,746 discloses the use of sulfur- amides activated by a carbonyl or sulfonyi group.adjacent to the

sulfurarnide nitrogen in the process of sweetening sour hydrocar¬ bon distillates.

U. S. Patent Number 4,039,586 discloses a process for oxi¬ dizing organic thiols to disulfides whereby the- organic thiol is reacted with a xanthide in the presence of a tertiary amine.

^■ U. S. Patent Numbers 4,048,097; 4,078,992 and 4,088,569 disclose the use of an ammonium donor in the preparation of metal phthalocyanine catalyst composites.

U. S. Patent Numbers 4,100,057; 4,142,964 and 4,168,245 disclose the use of small amounts of morpholine in the catalytic sweetening of sour petroleum distillate.

U. S. Patent Numbers 4,121,997; 4,124,493; 4,124,494 4,127,474; 4,156,641; 4,157,312; 4,159,964; 4,203,827; 4,206,079 4,213,877; 4,250,022; 4,260,479; 4,276,194; 4,290,913 4,290,916 4,290,917; 4,293,442; 4,295,993; 4,298,463; 4,299,729 and 4,308,169 disclose the use of ionic, quaternary ammonium com¬ pounds in processes for oxidizing mercaptan compounds.

U. S. Patent Number 4,207,173 discloses the use of a tetra— alkyl guanidine to supply the basic medium instead of an aqueous sodium hydroxide solution customarily used in the processes for sweetening sour hydrocarbons .

U. S. Patent Number 4,502,949 discloses a process for sweet¬ ening sour hydrocarbons whereby the mercaptans contained in the hydrocarbon are reacted with an oxidizing agent by contacting the hydrocarbon and oxidizing agent with a supported metal chelate

mercaptan oxidation catalyst and anhydrous ammonia in the absence of an aqueous phase.

U. S. Patent Number 4,514,286 discloses a process for reduc¬ ing the mercaptan concentration of a sour petroleum distillate by contacting the distillate with a hydroperoxide compound and a quaternary ammonium hydroxide salt.

The above-listed patents are also incorporated by reference herein for all purposes as if fully set forth.

None of the above-described processes or nitrogen compounds as utilized in those processes is applicable for use in a variety of processes or as both a promoter for extraction and catalytic oxidation. For example, the use of high concentrations of nitro¬ gen compounds in the hydrocarbon stream as taught by some of the references may result in unwanted color problems with the pro¬ duct. Other of the processes are not applicable in conventional hydrocarbon caustic oxidizing agent oxidation catalyst systems which dominate the sweetening and regeneration operations. Fur¬ ther, many of the processes are not easily adaptable to such conventional systems.

It has now been surprisingly discovered that the extraction and catalytic oxidation of the mercaptan compounds is promoted by the addition of small amounts of selected nitrogen-based com¬ pounds, as described hereinafter. It has also been surprisingly discovered that such nitrogen-based compounds may be utilized in a variety of sweetening and regeneration processes, as is also described hereinafter.

The object of the invention is to provide methods for treating streams having mercaptan or mercaptan-based compounds therein. The methods comprise, in their broadest concept, contacting a first stream having the mercaptan or mercaptan-based compounds therein with a second stream to either: (1) convert the mercaptan or mercaptan-based com¬ pounds to disulfide compounds; (2) extract the mer¬ captan, mercaptan-based or disulfide compounds; or (3) combinations thereof.

The first stream is either a sour hydro¬ carbon distillate or a spent caustic solution. If the first stream is a sour hydrocarbon distillate, the second stream is a caustic solution, and if the first stream is a spent caustic solution, the second stream is a hydrocarbon solvent.

Specifically, the invention provides a method of treating a first stream having mercaptan or mercaptan-based compounds therein by contacting said first stream with a second stream, wherein said mercaptan or mercaptan-based compounds are either extracted, catalytically oxidized to disulfide compounds, or both, wherein said first stream is either a sour hydrocarbon distillate or a spent caustic solution; provided if said first stream is a sour hydrocarbon distillate said second stream is a caustic solution, and if said first stream is a spent caustic solution said second stream is a hydrocarbon distillate, characterized by contacting said first and second streams in the presence of from about 1 ppm to about 50 ppm by weight, based upon the hydro- . carbon steam of a mitrogen-based promoter comprising a non-electrolytic, substantially sulfur free organic compound having at least one nitrogen atom, said nitrogen-based promoter being selected from the group consisting of: heterocyclic

compounds, wherein the ring or rings of said hetero- cycliσ compounds consist of carbon and nitrogen atoms; substituted homocyclic compounds, wherein at least one substituent attached to the ring or rings of said homocyclic compounds comprises at least one nitrogen atom; aliphatic compounds comprising at least one nitrogen atom; and mixtures thereof. More preferably from about 1 ppm to about 10 ppm by weight of the nitrogen-based promoter is utilized and most preferably from about 4 to 6 ppm. The heterocyclic compounds preferably comprise from about 3 to about 40 atoms, more preferably from about 4 to about 24 atoms, in the ring or rings thereof, while the homocyclic compounds more preferably comprise from about 3 to about 34 atoms, preferably from about 5 to about 24 atoms, in the ring or rings thereof. Add¬ itional methods for treating streams as well as sweetening sour hydrocarbon distillates are provided for.

The most preferred nitrogen-based promoters comprise those listed in Example 7 hereinafter.

The present invention is particularly adapted to the processes for sweetening sour hydro¬ carbon distillate by the catalytic oxidation of the mercaptan or mercaptan-based compounds, sweetening sour hydrocarbon distillates by the extraction of the mercaptan or mercaptan-based compounds, and regener¬ ating spent caustic solutions containing mercaptides.

The present invention is also applicable in a variety of apparatus and the processes specifically adapted therefor. For example, the invention may be utilized in continuous, batch, cocurrent, counter- current and the like operations; liquid-liquid, liquid-vapor, etc. processes; packed tower, bubble tray, stirred vessel, fiber contacting and other similar apparatus; fixed-bed catalyst.

aqueous catalyst, etc. systems; and other variants too numerous to list. The invention, therefore, is applicable in most processes and apparatus relating to the sweetening of sour hydrocarbons and the regeneration of spent caustic solutions.

The advantages of the present invention is readily understood by those skilled in the art with reference to the accompanying drawings.

Fig. 1 illustrates a general schematic of a cocurrent liquid-liquid fiber mass transfer apparatus useful in the practice of this invention.

Fig. 2 illustrates a general schematic of a combination fiber bundle/fixed bed liquid-liquid mass transfer apparatus useful in the practice of this invention.

Fig. 3 illustrates a general schematic of a countercurrent liquid-liquid fiber mass transfer apparatus useful in the practice of this invention.

A stated, the present invention provides methods for treating streams containing mercaptan and mercaptan-based compounds. Mercaptan compounds are commonly defined, and defined for the purpose of this description, as hydrosulfide compounds containing the radical -SH. Mercaptan-based compounds are defined for the purposes of this description as derivatives of mercaptans such as, for example, mercaptides and disulfides. The present inventions particularly adapted for sweetening mercaptan-containing sour hydrocarbon distillate and regenerating spent caustic solutions utilized to extract mercaptan compounds from such distillate.

The invention, in its broadest sense, comprises an improve¬ ment over prior art sweetening and regeneration processes through the utilization of small amounts of nitrogen-based compounds as promoters for the extraction and oxidation reactions. A promoter is commonly defined as an accelerator, and is herein utilized to designate both an accelerator for the catalyst utilized in the many embodiments of the invention and as an extraction enhancer. The nitrogen-based promoters as used in the practice of this invention, therefore, both enhance the extraction of mercaptan- based compounds and accelerate the catalytic oxidation of such to provide improved sweetening and regeneration capabilities at minimum extra expense.

As previously mentioned, the improvement of this invention is particularly adapted for use in a variety of sweetening and regeneration processes. For example, in the process of sweet¬ ening sour hydrocarbon streams by the catalytic oxidation of the mercaptans to disulfides, the sour hydrocarbon stream is contac¬ ted with a caustic stream, oxidizing agent and mercaptan oxida¬ tion catalyst in the presence of a nitrogen-based promoter at a temperature and pressure and for a time sufficient to oxidize a portion of the mercaptans. The catalytic oxidation process has both extraction and oxidation aspects, as the mercaptans are extracted into the caustic stream in the form of mercaptides, wherein the mercaptides are oxidized to disulfides then back .extracted into the hydrocarbon stream. The nitrogen-based

promoters, through an unknown mechanism, promote both the extrac¬ tion and oxidation steps.

Preferred operating temperatures range from about 60°F to about 200°F, more preferably from about 90°F to about 150°F, while preferred operating pressures range from atmospheric up to about 15 atmospheres. The actual reaction conditions, of course, depend on the specific sweetening process chosen as will be recognized by those skilled in the art.

The caustic stream is preferably an aqueous alkali metal hydroxide solution, most preferably sodium or potassium hydrox¬ ide, having a concentration of from about 5% to about 50%, more preferably from about 5% to about 25%, still more preferably from about 10% to about 20%, by weight alkali hydroxide. Such caustic solutions are widely used for the treatment of a variety of mercaptan containing hydrocarbon streams including, but not limi¬ ted to, liquid petroleum gas (LPG) , butanes, butenes, gasoline streams, jet fuels, kerosenes, naphthas and the like. The afore¬ mentioned hydrocarbon streams can typically contain a number of different mercaptan sulfur compounds, including, but not limited to, methyl mercaptan, ethyl mercaptan, n-propyl mercaptan, iso- propyl mercaptan, n—butyl mercaptan, thiophenol and other branched and/or higher molecular weight mercaptans.

The oxidizing agent is preferably an oxygen containing gas, most preferably air, and is usually dissolved in the sour hydro- carbon stream prior to contact with the caustic stream but may be bubbled therethrough after contact. The oxidizing agent is

preferably present in at least the stoichiometic amount necessary to oxidize all of the mercaptans, most preferably from about 100% to about 500% of the stoichiometric amount.

The mercaptan oxidation catalyst is preferably a metal che- late, more preferably a metal phthalocyanine. Any suitable phthalocyanine catalyst meeting the requirements of high activity and stability during use may be employed in the present inven¬ tion. The catalyst is usually present as either being in solu¬ tion with the caustic stream or as a composite in a fixed bed. Particularly preferred metal phthalocyanines include cobalt phthalocyanine and vanadium phthalocyanine; however, if the cata¬ lyst is to be soluble in the caustic stream, it is preferred that the catalyst be a phthalocyanine derivative, more preferably sulfonated and carboxylated derivatives, most preferably the disulfonated derivatives. Thus, the preferred catalyst comprises either cobalt phthalocyanine disulfonate or vanadium phthalocya¬ nine disulfonate.

If the catalyst is in solution with the caustic stream, the preferred concentration of the catalyst is between about 5 ppm and about 1000 ppm, more preferably between about 5 ppm and about 500 ppm, still more preferably between about 10 ppm and about 200 ppm, by weight based on the caustic stream.

In addition to the mercaptan oxidation catalyst being in solution with the caustic stream, the catalyst, preferably a similar phthalocyanine catalyst, may be in the form of a compo¬ site with a suitable support. The support should be insoluble

in, or substantially unaffected by the caustic stream and hydro¬ carbons under the conditions prevailing during the contact of the streams. Activated carbon is particularly preferred because of its high adsorptivity and stability under these conditions. Other carbon carriers include coke, charcoal which may be obtained from any suitable source including bone char, wood charcoal, charcoal made from cocoa-nut or other nut shells, fruit pits and similar sources. The choice of support will be made with reference to its adsorptive or spacing properties and its stability in the caustic stream and hydrocarbon stream under the reaction conditions as will be understood by those skilled in the art.

The composite of phthalocyanine and support may be prepared in any suitable manner. In one method the support may be formed into particles of uniform or irregular size and shape including spheres, prills, pellets, rings, saddles, flakes and the like and is then intimately contacted with a solution of phthalocyanine catalyst. An aqueous solution of phthalocyanine catalyst is prepared and, in the preferred embodiment, the support particles are soaked, dipped, suspended or immersed in the solution. In another method, the solution may be sprayed onto, poured over or otherwise contacted with the support. Excess solution may be removed in any suitable manner, and the support containing the catalyst is typically dried at temperatures of 180°F and above, in an oven, by means of hot gases passed thereover or in any other suitable manner.

In general, it is preferred to composite as much catalyst with the support as will form a stable composite although a lesser amount may be so deposited if desired. In a typical preparation, about 1% by weight of phthalocyanine catalyst is composited with activated carbon by soaking granules of the carbon in a solution of phthalocyanine catalyst.

The nitrogen-based promoters are preferably introduced into the system as being dissolved in the sour hydrocarbon streams in amounts from about 1 ppm to about 50 ppm, more preferably from about 1 ppm to about 10 ppm, most preferably from about 4 to about 6 ppm, by weight based upon the hydrocarbon stream. The nitrogen-based promoters may also be added to the system after contact of the hydrocarbon and caustic streams, or may be added to the caustic stream prior to contact with the hydrocarbon stream.

The nitrogen-based promoters preferably comprise non- electrolytic, substantially sulfur free organic compounds having at least one nitrogen atom and selected from the following groups: (1) heterocyclic compounds, wherein the ring or rings thereof consist of carbon and nitrogen atoms; (2) substituted homocyclic compounds, wherein at least one of the substituents attached to the ring or rings thereof comprising at least one nitrogen atom; (3) aliphatic compounds comprising at least one nitrogen atom; and (4) mixtures thereof. Non-electrolytic com¬ pounds are commonly defined, and defined for the purposes of this invention, as those compounds that do not easily dissociate into

two or more ions in water. The heterocyclic compounds further preferably comprise from about 3 to about 40 atoms, more preferably, from about 4 to about 24 atoms, in the ring or rings thereof, and the homocyclic compounds further preferably comprise from about 3 to about 34 atoms, more preferably from about 5 to about 24 atoms, in the ring or rings thereof.

A representative, but by no means exhaustive, list of hete¬ rocyclic compounds useful in the practice of this invention is as follows: pyridine, picolene, nicotinonitrile, 1-phenol pyrrole, phenazine, pyradazine, pyrimidine, 2,2-bipyridine, quinoline, 2,2-biquinoline, methylpyrimidine, 2,4,6-triaminopyrimidine, triazine, melamine, methenamine, 3,4-diaminopyridine, 3-amino- pyridine, acridine, quinaldine, isoquinoline, 4—aminopyrazolo [3,4-d] pyrimidine, 3-aminoquinoline, 7—azaindole, 5-triazolo [4, 3-a] quinoline, 4-azabenzimidazole, pyrido (2,3-b) pyrazine, L- histidine, aminopiperidine, 2,2'-biquinoline, benzotriazole, qui- noxaline, 1,2,4—triazole, 5-aminoindazole, triethylenediamine, aminopyrazole, 5, 10, 15,20-tetraρhenyl 21H,23H porphine, pyrazine, aminopyrazine, 2-methylpyrazine, nicotine, 2-analinopyridine, 2- aminopyrimidine, 4-dimethylamiπopyridine, benzimidazole, N- methyltolyimidazole, tolyimidazole, pyrrole, pyrrolidine, 4— methylpiperidine, 2,5 dimethylpyrrole, piperidine, 1- ethylpiperidine, 2-ethylpiperidine, piperazine, pyrazole, indole, 3— ethylindole, 5-methylindole, indoline, polyvinyl piperidine, azabicyclo (3.2.2) nonane, phthalocyanine, homopiperazine, 1,4,8,12 tetraazacyclopentadicane, 5-aminoindole, carbazole,

imidazole, N-alkylate imidazole, skatole, quinalidine, purine,

2,3-cyclopentenepyridine, penanthroline, etc.

A representative, but again by no means exhaustive, list of homocyclic compounds useful in the practice of this invention is as ollows: N ,N -dimethylbenzylamine, 4-aminopyrene, aniline,

1 1 2,5-dimethylaniline, 2,4-diaminotoluene, toluidine, cyclohex- amine, tolunitrile, nitrobenzene, cyclopentylamine, cyclobutyl- amine, cyclopropylamine, 4-cyclohexylaniline, cyclooctylamine, aminoindane, napthylamine, amitriptyline, etc.

A representative, but once again by no means exhaustive, list of aliphatic nitrogen compounds useful in the practice of this invention is .as follows: methylamine, urea, T-octylamine, octadecylamine, ethylenedia ine, L-isoleucine, triethylene tetra- mine, butylamine, N-heptyl cyanide, etc.

The most preferred of these nitrogen compounds are 1-phenyl- pyrrole, pyradazine, pyrimidine, methylpyrimidine, methenamine, 3-aminoquinoline, s-tiazolo [4,3-a] quinoline, 4-azabenzimida¬ zole, pyridopyrazine, 1,3,5 triazine, benzotriazole, pyrazine, 2- aminopyrimidine, 4-methylpiperidine, piperidine, azabicyclo [3,2,2] nonane, and 2, -diaminotoluene.

As previously mentioned, the nitrogen-based promoters are utilized in amounts from about 1 ppm to about 50 ppm by weight based upon the hydrocarbon stream. Use of excess nitrogen-based promoter may cause unwanted problems such as, for example, color impurities which can result in a less desirable product, and may

in fact decrease the efficiency of the use of the nitrogen-based compounds as promoters .

Also as previously mentioned, the nitrogen-based promoters are non-electrolytic. Because of this non-electrolytic nature, ⁵ the promoters will be preferentially soluble in the hydrocarbon stream. As most hydrocarbon product specifications set an upper limit to the amount of sulfur allowable in the hydrocarbon pro¬ duct, it is highly desirable not to add additional sulfur to the hydrocarbon in any form. The nitrogen-based promoters, there- ⁰ fore, are not only non-electrolytic but also substantially sulfur free.

The improvement of this invention is also adapted for use in the process of sweetening sour hydrocarbon streams by the strict extraction of the mercaptan compounds therein, wherein the sour

¹⁵ hydrocarbon stream is contacted with a caustic stream in the presence of the aforementioned nitrogen-based promoters at a temperature and pressure and for a time sufficient to extract at least a portion of the mercaptans. The temperature, pressure and composition of the caustic stream are preferably similar to the nr\

^ ^u sweetening by catalytic oxidation process as discussed above; however, the exact process conditions again depend on which of the variety of processes is practiced with the invention as will be understood by those skilled in the art.

As earlier noted, the promoters, through an unknown mecha-

25 nism, promote the extraction of the mercaptans from the hydrocar¬ bon stream to the caustic stream in the form of mercaptides,

which are preferentially soluble in the caustic stream. The caustic stream is then separated from the hydrocarbon stream, leaving a sweetened hydrocarbon product.

The resulting caustic stream is usually recycled in the extraction process until it is spent, that is, until the capacity of the caustic stream to extract mercaptans is so diminished that the process no longer runs efficiently. The spent caustic stream is then either discarded or regenerated for reuse.

In the regeneration process the mercaptide-containing caus¬ tic stream is contacted with a hydrocarbon stream, an oxidizing agent and a mercaptan oxidation catalyst in the presence of a nitrogen-based promoter.. The composition of the oxidizing agent, mercaptan oxidation catalyst and nitrogen-based promoter and the reaction conditions are preferably the same as described above for the sweetening by catalytic oxidation process, and again specifically depend upon the process chosen with which to prac¬ tice the invention as will be understood by those skilled in the art.

The present invention is also applicable in a variety of apparatus and the processes specifically adapted therefor. For example, this invention may be utilized in continuous, batch, cocurrent, countercurrent and the like operations; liquid-liquid, liquid-vapor, etc. processes; packed tower, bubble tray, stirred vessel, fiber contacting and other similar apparatus; fixed-bed catalyst, aqueous catalyst, etc. systems; and other variants too numerous to list. The invention, therefore, is applicable in

most processes and apparatus relating to the sweetening of sour hydrocarbons and the regeneration of spent caustic solutions.

Referring now to Fig. 1, there is illustrated a general schematic of a cocurrent liquid-liquid mass transfer apparatus useful in the practice of this invention. The apparatus of Fig. 1 makes use of the mass transfer techniques and apparatus as disclosed in U. S. Patent Numbers 3,977,829 and 3,992,156, and reference may be made to such patents for a full description thereof. It should here be noted that the present invention is not to be limited by its use with the apparatus of Fig. 1 nor is the use of the apparatus of Fig. 1 to be limited to the specific processes hereinafter described.

The mass transfer apparatus M of Fig. 1 includes a bundle. B of substantially continuous elongated fibers 6 mounted in a shroud S and contained within conduit 10. Conduit 10 is provided with an inlet flange 10a that is adapted for connection or place¬ ment with mounting flange 9a of conduit inlet assembly 9. A fluid distribution means 12 is mounted within conduit inlet assembly 9 for distributing the caustic stream from caustic feed line 8 onto fibers 6 of fiber bundle B. ^• A hydrocarbon feed line 14 is also attached to conduit inlet assembly 9 for delivering the hydrocarbon stream into conduit assembly 9.

Conduit 10 is also provided with an outlet flange 10b which is adapted for placement or connection with mounting flange 11a of collection vessel 11. Collection vessel 11, during the opera¬ tion of mass transfer apparatus M, will contain a lower layer 18

of caustic solution and an upper layer 20 of hydrocarbon solution resulting from the processes of this invention as described hereinafter. Shroud S and fibers 6 of fiber bundle B extend partly within the confines of collection vessel 11, with the positioning of the downstream end 16 of fiber bundle B within collection vessel 11 being such that downstream end 16 is within the caustic solution collected as lower layer 18.

Fibers 6 that comprise fiber bundle B are selected to meet two criteria: (1) the fiber material must be preferentially wetted by the caustic solution introduced by feed line 8; and (2) the fibers must be of a material that will not contaminate the process or be destroyed by it, such as by corrosion. According¬ ly, inasmuch as the processes of this invention deal with caustic solutions and hydrocarbons containing sulfur compounds, metallic fibers and, in particular, stainless steel or special corrosion resistant alloy fibers, are preferably employed.

A -first specific embodiment of the invention utilizes the apparatus of Fig. 1 for sweetening sour hydrocarbon streams by the catalytic oxidation of the mercaptan compounds therein. A second specific embodiment of the invention utilizes the appara¬ tus of Fig. 1 for sweetening sour hydrocarbon streams by the extraction of the mercaptan compounds therein. A third specific embodiment of the invention utilizes the apparatus of Fig. 1 for regenerating spent caustic solutions utilized in a mercaptan extraction process. Specific mechanical and operational details of mass transfer apparatus M will be provided below with the

description of each specific embodiment of the invention. Other mechanical details of the mass transfer apparatus M not necessary to an understanding of the invention may be had by reference to the aforementioned patents.

In order to sweeten mercaptan-containing sour hydrocarbon streams according to the first specific embodiment, the caustic stream containing an oxidation catalyst is flowed through caustic feed line 8, into inlet assembly 9, to fluid distribution means 12 and onto the upstream end Bl of the fiber bundle B as illus¬ trated in Fig. 1. Simultaneously, the sour hydrocarbon stream containing the nitrogen—based promoter and a dissolved oxygen- containing gas, such as air, is flowed through hydrocarbon feed line 14, into inlet assembly 9, and then cocurrently with and in intimate contact with the caustic stream, passing over fibers 6 of fiber bundle B contained within conduit 10, and then into collection vessel 11. _^ During the time the two immiscible fluids are in contact within conduit 10, the mercaptans contained in the hydrocarbon stream are extracted into the caustic as mercaptides, oxidized to disulfides, then back-extracted into the hydrocarbon stream and are thus removed from the caustic solution.

The caustic streams herein utilized include, for example, aqueous potassium hydroxide solutions and aqueous sodium hydrox¬ ide solutions having concentration of from about 5% to about 50%, more preferably from about 5% to about 25%, still more preferably from about 10% to about 20%, by weight alkali hydroxide.

As previously mentioned, fibers 6 must be preferentially wetted by the caustic stream introduced by caustic feed line 8. If, however, the volumetric flow ratio of the hydrocarbon stream to caustic stream is less than about 1:1, phase inversion may occur resulting in fibers 6 being preferentially wetted by the hydrocarbon stream. It is preferred, therefore, that the volume¬ tric flow ratio of the hydrocarbon stream to caustic stream be at least about 1:1, more preferably from about 2:1 to about 20:1, still more preferably about 3:1 to about 7:1, most preferably about 5:1.

The oxidation reaction will occur at temperatures of from ambient to about 200°F. The preferred operating temperature is from about 100°F to about 130°F.

The oxidation reaction is relatively fast, however, suffi¬ cient time must be allowed for the mercaptans and/or oxygen to be transferred to the caustic stream and for the resulting disul¬ fides to be transferred back into the hydrocarbon stream. Because of the efficiency of mass transfer apparatus M, residence time in fiber bundle B may be rather short, generally from about thirty seconds to about three minutes. Preferred residence times are from about one to about two minutes.

The oxidation catalyst contained in the caustic stream may be any suitable oxidation catalyst known to those skilled in the art and preferably comprises a metal phthalocyanine dissolved or suspended in the caustic stream entering the system through caustic feed line 8. Metal phthalocyanines that may be employed

include cobalt phthalocyanine and vanadium phthalocyanine or sulfonated or carboxylated derivatives thereof. A preferred catalyst comprises cobalt phthalocyanine disulfonate. The cata¬ lyst concentration will vary depending in part on the level of mercaptans in the hydrocarbon stream, as will be understood by those skilled in the art. Typically, the amount of phthalocya¬ nine catalyst may range from about 10 ppm to about 1000 ppm, more preferably from about 10 ppm to about 500 ppm, still more prefer¬ ably from about 10 ppm to about 200 ppm, by weight based upon the caustic stream.

The oxygen required for the oxidation of the mercaptans is introduced into the system through line 15 by dissolving oxygen or an oxygen-containing gas, such as air, in the hydrocarbon stream. In fiber bundle B, the oxygen is transferred from the hydrocarbon stream into the caustic stream. Oxygen thus is available for chemical reaction with the mercaptides in the presence of the oxidation catalyst contained in the caustic stream as the respective fluids move through fiber bundle B of mass transfer apparatus M. The amount of oxygen provided is at least equal to the s-toichiometric amount required to oxidize all of the mercaptans to disulfides and generally is provided in excess of the stoichiometric amount, usually up to about 500% of the stoichiometric amount. The pressure in the system is main¬ tained at a level such that the desired amount of oxygen can be dissolved into the hydrocarbon stream without exceeding the

solubility limits for oxygen or the oxygen-containing gas in the hydrocarbon.

The higher the mercaptan concentration of the sour hydrocar¬ bon stream, the more oxygen or Oxygen—containing gas must be d ^' issolved in the hydrocarbon, and higher system back pressure must be maintained in order to keep such amounts of oxygen- containing gas in solution. Typical system back pressures range from 10 psig to 100 psig with system back pressures of from about 25 psig to about 75 psig typically being sufficient for most normal mercaptan loadings .

The nitrogen-based promoters, the details of which have previously been described, are introduced into the system by injection through line 14a into the hydrocarbon stream. The nitrogen-based promoters are added to the hydrocarbon streams in amounts of from about 1 ppm to about 50 ppm, more preferably from about 1 ppm to about 10 ppm, most preferably from about 4 to about 6 ppm, by weight based upon the hydrocarbon stream.

The downstream end SI of shroud S containing the fiber bundle B extends into collection vessel 11 sufficiently so as to allow end 16 of fiber bundle B to contact caustic lower layer 18. Thus, as the caustic and hydrocarbon streams flow from conduit 10 into collection vessel 11, the caustic stream, being immiscible with the sweetened hydrocarbon, separates and collects as lower layer 18 and the hydrocarbon stream, now containing disulfides, accumulates as upper layer 20 in collection vessel 11. Collec¬ tion vessel 11, therefore, is preferably maintained at conditions

which avoid entrainment of the hydrocarbon and caustic streams. The interface 21 between the hydrocarbon and caustic may vary, but it is preferred that the interface remain above end 16 of fiber bundle B as illustrated in Fig. 1. As a result of the oxidation of mercaptans to disulfides within fiber bundle B, a sweetened hydrocarbon is produced.

The sweetened hydrocarbon and caustic streams are withdrawn separately from the collection vessel 11. The caustic stream is withdrawn through caustic outlet line 17 and may be recycled for further use, for example, in further contacting of mercaptan- containing hydrocarbon streams. In a typical system, it may be necessary from time to time to purge some of the caustic solution from the recirculation loop through purge line 17a and replace it with fresh caustic solution from fresh caustic line 7. This is generally done as needed to control the buildup of carbonates from CO in the oxidation air and thiosulfates and other sulfur

2 compounds which may be present in the system due to the presence of hydrogen sulfide in the hydrocarbon stream. The addition of fresh caustic solution may also be necessitated due to the dilu¬ tion effect resulting from the oxidation of the mercaptans where¬ in water is a co-product of the oxidation reaction.

The hydrocarbon stream is withdrawn from collection vessel 11 through hydrocarbon outlet line 19 and may be recovered through product line 19a or may be recycled to hydrocarbon feed line 14 for further treatment. In the latter event, it may be necessary to pass the hydrocarbon stream through a degassing zone

30 wherein the pressure is reduced by a suitable pressure relief valve P to enable the dissolved gases, primarily nitrogen if air is used as the oxygen source, to come out of solution and be separated therefrom through vent 31. This, of course, would not be necessary if oxygen itself were used in stoichiometric quanti¬ ties for the oxidation.

It should here be noted that the catalytic sweetening pro¬ cess as detailed in this first specific embodiment may, for example, also be utilized in an apparatus similar to the one depicted in Fig. 1 except that the hydrocarbon and caustic streams are contacted in the presence of a fixed bed catalyst (not shown) as previously described instead of fiber bundle B. The process operating conditions are essentially the same in either the fixed bed or fiber bundle apparatus except that the oxidation catalyst is contained within the fixed bed instead of, or in addition to, in solution with the caustic stream.

The sweetening process as previously described may also be utilized in an apparatus having both a fiber bundle and fixed bed catalyst contacting section, such as the apparatus disclosed and described in U. S. Patent Application Serial No. 739,563, f led May 30, 1985, assigned to the assignee of the present invention and incorporated by reference herein for all purposes as if fully set forth. Such an apparatus is especially effective for tre¬ ating streams having difficultly oxidizable mercaptans.

Referring now to Fig. 2, there is illustrated a schematic of a combination fiber bundle/fixed bed apparatus A such as

disclosed and described in the above-mentioned patent applica¬ tion. Apparatus A includes a fiber bundle F of substantially continuous elongated fibers 50 contained within conduit 52. A fluid distribution means 54 is mounted within conduit 52 for distributing the caustic stream from caustic feed line 56 onto fibers 50 of fiber bundle F. A hydrocarbon feed line 58 is also provided for delivering the hydrocarbon stream into conduit 52.

At the downstream end 52a of conduit 52 is a collection vessel 60 into which the downstream end 50a of fibers 50 extend. Collection vessel 60 is preferably integrated with the vessel V enclosing conduit 52.

Collection vessel 60, during the operation of apparatus A, contains a lower layer 62 of caustic solution and an upper layer 64 of hydrocarbon solution. Downstream end 50a of fibers 50 are positioned within collection vessel 60 such that downstream end 50a is within the caustic solution collected as lower layer 62.

Apparatus A is also provided with a fixed catalyst bed C preferably in annular arrangement around conduit 52. Fixed cata¬ lyst bed C comprises a mercaptan oxidation catalyst composited on a suitable support, such as the supported catalysts previously described. Catalyst bed C is supported in vessel V by a restraining means 70 such as a screen or other suitable device as will be recognized by those skilled in the art.

Other mechanical details of apparatus A are not necessary to an understanding of the invention. Most of the operating parame¬ ters of apparatus A, such as the caustic and hydrocarbon stream

compositions, operating temperatures and pressures, and composi¬ tions of the oxidizing agents, mercaptan oxidation catalysts and nitrogen-based promoters, are essentially the same as in appara¬ tus M of Fig. 1, the details of which have previously been dis¬ cussed and to which reference may be made.

In order to sweeten mercaptan-containing compounds utilizing apparatus A of Fig. 2, a caustic stream containing a mercaptan oxidation catalyst is flowed through caustic feed line 56 to fluid distribution means 54 and onto the upstream end Fl of fiber bundle F. Simultaneously, the sour hydrocarbon stream containing the nitrogen-based promoter and oxidizing agent is flowed through hydrocarbon feed line 58, into conduit 52 and then cocurrently with and in intimate contact with the caustic stream, passing over fibers 50 of fiber bundle F and then into collection vessel 60. During the time the hydrocarbon and caustic streams are in contact, a portion of the mercaptans is catalytically oxidized to disulfides. As the caustic and hydrocarbon streams flow from conduit 52 into collection vessel 60, the caustic stream, being immiscible with the hydrocarbon stream, separates and collects as lower -layer 62 while the hydrocarbon stream, now having disul¬ fides and the remaining mercaptans therein, accumulates as upper layer 64 in collection vessel 60. The interface 63 within col¬ lection vessel 60 is preferably kept at a level above downstream end 50a of fibers 50 so that the caustic stream can be collected directly in the bottom of collection vessel 60 without it being dispersed into the hydrocarbon stream.

The caustic stream is withdrawn through caustic outlet line 66 and may be recycled for further use. In a typical system, it may be necessary from time to time to purge some of the caustic solution from the recirculation loop through purge line 66a and replace it with fresh caustic from fresh caustic line 56a for essentially the same reasons as mentioned in relation to the other catalytic oxidation processes.

The hydrocarbon stream, upon disengagement from fiber bundle F and collection as upper layer 64, moves up through catalyst bed C, wherein it is contacted by fresh caustic introduced into catalyst bed C from fresh caustic line 68a through distributors 68 placed within catalyst bed C. While placement of distributors 68 ^' is arbitrary within catalyst bed C, they should be placed toward the top 25% of the bed to allow suf icient contact between the caustic and the remaining mercaptans in the hydrocarbon stream. The fresh caustic is preferably the same composition as the other caustic solutions utilized herein and may or may not contain a mercaptan oxidation catalyst depending upon such fac¬ tors as the amount and type of mercaptans remaining in the hydro— carbon stream and the efficiency of the catalyst in catalyst bed

C, as will be understood by those skilled in the art. The caus¬ tic stream exits catalyst bed C through restraining means 70 into collection vessel 60, wherein it settles and is accumulated into lower layer 62.

The sweetened hydrocarbon is removed from catalyst bed C and vessel V through hydrocarbon outlet line 72 via collection means

74, which can be any means suitable for removing the hydrocarbon stream from vessel V, as will be recognized by those skilled in the art. The hydrocarbon stream may then be removed as product through hydrocarbon product line 72a or may be recycled into hydrocarbon feed line 58 for further treatment. In the latter event, and under certain conditions as earlier detailed, it may be necessary to pass the hydrocarbon stream through a degassing zone (not pictured) where the pressure is reduced by a suitable pressure relief valve to enable any dissolved gases to come out of solution with the hydrocarbon stream and be separated there¬ from.

The use of the nitrogen-based promoters in conjunction with the first specific embodiment and modifications thereof signifi¬ cantly increases the efficiency of the sweetening processes as indicated by the examples presented hereinafter. The efficiency of these sweetening processes will also depend on a number of other parameters such as, for example, including the rates of mass transfer of oxygen into the caustic stream to provide the oxygen for the catalytic oxidation of the mercaptans, the rate of flow of streams entering the feed lines, the amounts of dissolved oxygen in the hydrocarbon stream, the amount of catalyst con¬ tained in the caustic stream, residence time of the respective materials within the mass transfer apparatus, temperature and pressure conditions, the chemical composition of sulfur compounds contained in the hydrocarbon stream to be sweetened, the type of caustic stream used, and other factors as will be recognized by

those skilled in the art. Based on the improved results utiliz¬ ing the nitrogen-based promoters, one skilled in the art will know how to adjust these parameters accordingly.

The second specific embodiment of this invention, as pre- viously mentioned, utilizes the apparatus of Fig. 1 for sweeten¬ ing sour hydrocarbons by the extraction of the mercaptan compounds therein. Referring again to Fig. 1, in order to swee¬ ten mercaptan-containing sour hydrocarbon streams according to the second specific embodiment, the caustic stream is flowed through caustic feed line 8 into inlet assembly 9 and to fluid distribution means 12 and onto upstream end Bl of fiber bundle B- as illustrated in Fig. 1. Simultaneously, the sour hydrocarbon stream containing the nitrogen-based promoter is flowed through hydrocarbon feed line 14, into inlet assembly 9, and then concur¬ rently with and in intimate contact with the caustic stream, passing over fibers 6 of fiber bundle B contained within conduit 10, and then into collection vessel 11. During the time the two immiscible fluids are in contact within conduit 10, the mercap¬ tans contained in the hydrocarbon stream are extracted into the caustic as mercaptides and are thus removed from the hydrocarbon stream.

As in the previous embodiments, the caustic streams utilized include, for example, aqueous potassium hydroxide solutions and aqueous sodium hydroxide solutions, having a concentration of from about 5% to about 50%, more preferably from about 5% to

about 25%, still more preferably from about 10% to about 20%, by weight alkali hydroxide.

Also as in the previous embodiments, fibers 6 must be pref¬ erentially wetted by the caustic stream introduced by caustic feed line 8. If, however, the volumetric flow ratio of the hydrocarbon stream to caustic stream is less than about 1:1, phase inversion may occur resulting in fibers 6 being preferen¬ tially wetted by the hydrocarbon stream. It is preferred, there¬ fore, that the volumetric flow ratio of the hydrocarbon stream to 0 caustic stream be at least about 1:1, more preferably from about 2:1 to about 20:1, still more preferably about 3:1 to about 7:1, most preferably about 5:1.

The extraction of the mercaptans from the hydrocarbon stream is relatively fast, however, sufficient time must be allowed for

^X ι ^ ^J the mercaptans to be transferred to the caustic stream as mercap¬ tides. Because of the efficiency of mass transfer apparatus M, residence time in the fiber bundle may be rather short, generally from about thirty seconds to about three minutes . Preferred residence times are from about one to about two minutes.

20 The nitrogen-based promoters, the details of which have previously been described, are introduced into the system by injecting the nitrogen-based promoters through line 14a into the hydrocarbon stream. The nitrogen-based promoters are added to the hydrocarbon streams in amounts of from about 1 ppm to about 50 ppm, more preferably from about 1 ppm to about 10 ppm, most preferably from about 4 to about 6 ppm, by weight based on the

hydrocarbon stream. The nitrogen-based promoters may also be added to the system after contact of the hydrocarbon and caustic streams, added to the caustic stream prior to contact with the hydrocarbon stream, or added in a solution with another hydrocar- bon diluent.

The downstream end SI of shroud S containing fiber bundle B extends into collection vessel 11 sufficiently so as to allow end 16 of fiber bundle B to contact caustic lower layer 18. Thus, as the caustic and hydrocarbon streams flow from conduit 10 into collection vessel 11, the caustic stream, being immiscible with the sweetened hydrocarbon, separates and collects as lower layer 18 and the hydrocarbon stream accumulates as upper layer 20 in collection vessel 11. Collection vessel 11 is, therefore, main¬ tained at conditions which avoid entrainment of the hydrocarbon and caustic streams. The interface 21 between the hydrocarbon and caustic may vary, but it is preferred that the interface remain above end 16 of fiber bundle B as illustrated in Fig. 1. As a result of the extraction of the mercaptan compounds into the caustic stream within the fiber bundle B, a sweetened hydrocarbon stream is produced.

The sweetened hydrocarbon and the caustic streams are with¬ drawn separately from collection vessel 11. The caustic stream is withdrawn through caustic outlet line 17 and may be recycled for further use, for example, in further contacting of mercaptan- containing hydrocarbon streams. The caustic stream may be recyc¬ led several times until it is spent, that is, until the capacity

of the caustic stream to extract the mercaptan compounds has diminished to such an extent as to make the process inefficient. In a typical system, therefore, it may be necessary from time to time to purge some of the caustic solution from the recirculation loop through purge line 17a and replace it with fresh caustic solution from fresh caustic line 7. The purged, or spent, caus¬ tic is normally discarded or regenerated for., reuse in the extrac¬ tion process by any one of a number of regeneration processes.

The sweetened hydrocarbon stream may be recovered through product line 19a or may be recycled to the inlet line 14 for further treatment.

The use of the nitrogen-based promoters in conjunction with the second specific embodiment and modifications thereof signifi¬ cantly increases the efficiency of the extraction processes as indicated by the examples presented hereinafter. The efficiency of these extraction processes will also depend on a number of other parameters such as, for example , the rate of flow of streams entering feed lines 8 and 14, residence time of the respective materials within mass transfer apparatus M, tempera- ture and pressure conditions, the chemical composition of sulfur compounds contained in the hydrocarbon stream to be sweetened, the type of caustic stream used, and other factors as will be recognized by those skilled in the art. Based on the improved results utilizing the nitrogen-based promoters, one skilled in in the art will know how to adjust these parameters accordingly.

The third specific embodiment of this invention, as previ¬ ously mentioned, utilizes the apparatus of Fig. 1 for regenerat¬ ing spent caustic solutions utilized in a mercaptan extraction process, such as, for example, the process described in the second specific embodiment.

The spent caustic streams which may be regenerated include, for example, spent aqueous potassium hydroxide solutions and spent aqueous sodium hydroxide solutions having an initial con¬ centration of from about 5% to about 50%, more preferably from about 5% to about 25%, still more preferably about 10% to about 20%, by weight alkali hydroxide. Such caustic solutions are widely used for treatment of a variety of mercaptan containing hydrocarbon streams, including liquid petroleum gas (LPG) , butanes, butenes, gasoline streams, jet fuels, kerosenes, naph¬ thas and the like. The spent caustic solutions resulting from the treatment of the aforementioned hydrocarbon streams can typi¬ cally contain a number of different mercaptan sulfur compounds, including, for example, such mercaptans as methyl mercaptan, ethyl mercaptan, n—propyl mercaptan, iso-propyl mercaptan, n- butyl mercaptan thiophenol and branched and/or higher molecular weight mercaptans. Alkali metal sulfides can also be in the spent caustic solutions due to the presence of hydrogen sulfide in the hydrocarbon streams which were previously treated with the alkaline solution. The presence of such does not adversely affect the efficiency of the present invention.

In order to regenerate mercaptide-containing caustic streams according to the third specific embodiment, the spent caustic stream containing an oxidation catalyst is flowed through caustic feed line 8 into the inlet assembly 9 and to fluid distribution means 12 and onto the upstream end Bl of the fiber bundle B as illustrated in Fig. 1. Simultaneously, a suitable hydrocarbon solvent containing the nitrogen-based promoter and a dissolved oxygen-containing gas such as air, is flowed through hydrocarbon feed line 14, into inlet assembly 9, and then cocurrently with and in intimate contact with the caustic stream, passing over fibers 6 of fiber bundle B contained within conduit 10, and then into collection vessel .11. During the time the two immiscible fluids are in contact within conduit 10, the mercaptides con¬ tained in the spent caustic solution are oxidized to disulfides then extracted into the hydrocarbon solvent and are thus removed from the caustic solution.

Again as previously mentioned, fibers 6 must be prefer¬ entially wetted by the caustic stream introduced by feed line 8. If, however, the volumetric flow ratio of the hydrocarbon solvent to caustic stream is less than about 1:1, phase inversion may occur resulting in fibers 6 being preferentially wetted by the hydrocarbon solvent. It is preferred, therefore, that the volu¬ metric flow ratio of the hydrocarbon solvent to caustic stream be at least about 1:1, more preferably from about 2:1 to about 20:1, still more preferably about 3:1 to about 7:1, most preferably about 5:1.

The oxidation reaction will occur at temperatures of from ambient to about 200°F. The preferred operating temperature is from about 100°F to about 130°F.

The oxidation reaction is relatively fast, however, suffi- cient time must be allowed for the oxygen to be transferred to the caustic stream and for the resulting disulfides to be trans¬ ferred back into the hydrocarbon stream. Because of the effi¬ ciency of the mass transfer apparatus, residence time in fiber bundle B may be rather short, generally from about thirty seconds to about three minutes. Preferred residence times are from about one to about two minutes.

The oxidation catalyst contained in the caustic stream may be any suitable oxidation catalyst known to those skilled in the art and preferably comprises a metal phthalocyanine dissolved or suspended in the caustic stream entering the system through caustic feed line 8. Metal phthalocyanines that may be employed include cobalt phthalocyanine and vanadium phthalocyanine or sulfonated or carboxylated derivatives thereof. A preferred catalyst comprises cobalt phthalocyanine disulfonate. The cata¬ lyst concentration will vary depending in part on the level of mercaptides in the caustic stream, as will be understood by those skilled in the art. Typically, the amount of cobalt phthalocya¬ nine disulfonate may range from about 10 ppm to about 1000 ppm, more preferably from about 10 ppm to about 500 ppm, still more preferably about 10 ppm to about 100 ppm, by weight based on the caustic solution.

The oxygen required for the oxidation of the mercaptides is introduced into the system through line 15 by dissolving oxygen or an oxygen-containing gas, such as air, in the hydrocarbon solvent. In fiber bundle B, the oxygen is transferred from the hydrocarbon solvent into the caustic stream. Oxygen thus is available for chemical reaction with the mercaptides in the presence of the oxidation catalyst contained in the spent caustic stream as the respective fluids move through fiber bundle B of mass transfer apparatus M. The amount of oxygen provided is at least equal to the stoichiometric amount required to oxidize all of the mercaptides to disulfides and generally is provided in excess of the stoichiometric amount, usually up to about 500% of the stoichiometric amount. The pressure in the system is main¬ tained at a level such that the desired amount of oxygen can be dissolved into the hydrocarbon stream without exceeding the solu¬ bility limits for oxygen or the oxygen-containing gas in the hydrocarbon.

The higher the mercaptide concentration of the spent caustic to be regenerated, the more oxygen or oxygen-containing gas must be dissolved in the hydrocarbon, and higher system back pressure must be maintained in order to keep such amounts of oxygen- containing gas in solution. Typical system back pressures range from 10 psig to 100 psig with system back pressures of from about 25 psig to about 75 psig typically being sufficient for most normal loadings .

The nitrogen—based promoters, the details of which have previously been described, are introduced into the system by injecting the nitrogen-based promoters through line 14a into the hydrocarbon solvent. The nitrogen-based promoters are added to the hydrocarbon in amounts from about 1 ppm to about 50 ppm, more preferably from about 1 ppm to about 10 ppm, most preferably from about 4 to about 6 ppm, by weight based on the hydrocarbon solvent.

Any suitable hydrocarbon solvent which is immiscible with the caustic stream and does not otherwise adversely affect the overall process may be utilized. For example, many of the hydro¬ carbon streams treatable for mercaptan removal with caustic streams may be employed as the solvent. Use of the hydrocarbon which has previously been treated by the caustic stream such as aromatics, gasoline, hexane, kerosene, naphtha or mixtures of any such organic solvents will avoid the possibility of contamination of the hydrocarbon stream by solvent which is entrained in the recirculating caustic stream.

The downstream end SI of shroud S containing fiber bundle B extends into collection vessel 11 sufficiently so as to allow end 16 of fiber bundle B to contact the regenerated caustic lower layer 18. Thus, as the caustic and hydrocarbon streams flow from conduit 10 into collection vessel 11, the regenerated caustic stream, being immiscible with the hydrocarbon, separates and collects as lower layer 18 and the hydrocarbon solvent, now containing disulfides, accumulates as upper layer 20 in

collection vessel 11. Collection vessel 11, therefore, is pref¬ erably maintained at conditions which avoid entrainment of the hydrocarbon and caustic streams. The interface 21 between the solvent and regenerated caustic solution may vary, but it is preferred that the interface remain above end 16 of fiber bundle B as illustrated in Fig. 1. As a result of the simultaneous oxidation of mercaptides to disulfides and extraction of the disulfides into the solvent within fiber bundle B, a regenerated caustic stream of reduced mercaptide content is produced.

The hydrocarbon and the regenerated caustic streams are withdrawn separately from the collection vessel 11. The regener¬ ated caustic stream is withdrawn through caustic outlet line 17 and may be recycled. for further treatment in the aforementioned regeneration process or for further use, for example, in contact¬ ing mercaptan-containing hydrocarbon streams. In a typical regeneration system, it may be necessary from time to time to purge some of the regenerated caustic solution from the recircu¬ lation loop and replace it with fresh or other spent caustic solution. This is generally done as needed to control the build¬ up of carbonates from CO in the oxidation air or thiosulfates or

2 other sulfur compounds which may be present in the system due to the presence of hydrogen sulfide in the hydrocarbon stream being treated with the caustic solution prior to the regeneration step. The addition of fresh or other spent caustic solution may also be necessitated due to the dilution effect resulting from the

oxidation of the mercaptides wherein water is a co—product of the oxidation reaction.

The hydrocarbon solvent containing disulfide compounds is withdrawn from collection vessel 11 through hydrocarbon outlet line 19 and may be processed further to recover the disulfide component therefrom, may be discarded in an environmentally safe manner, or may be recycled to hydrocarbon feed line 14 for fur¬ ther use in the process of the present invention. In the latter event, it may be necessary to pass the solvent solution through a ° degassing zone 30 wherein the pressure is reduced by a suitable pressure relief valve P to enable the dissolved gases, primarily nitrogen if air is used as the oxygen source, to come out of solution and be separated therefrom through vent 31. This, of course, would not be necessary if oxygen itself were used in 5 stoichiometric quantities for the oxidation. Also, since the solvent loses its effectiveness as the level of disulfides increases, it may be desirable to remove some of the disulfide- containing solvent through line 19 and to add fresh, lean solvent through line 23 from time to time in a continuous mode in order

2 * ^• 0 to maintain the proper efficiency of extraction of disulfides.

The use of the nitrogen-based promoters in conjunction with the third specific embodiment and modifications thereof signifi¬ cantly increases the efficiency of the regeneration processes as indicated by the examples presented hereinafter. The efficiency *~ of the regeneration processes will also depend on a number of other parameters such as, for example, the rates of mass transfer

of oxygen into the caustic stream to provide the oxygen for the catalytic oxidation of the mercaptides to disulfides, the rates of extraction of the resulting disulfide from the alkaline stream into the solvent, the rate of flow of streams entering feed lines 8 ^* and 14, the amounts of dissolved oxygen in either of the reactant streams, the amount of catalyst contained in the caustic stream, the residence time of the respective materials within mass transfer apparatus M, temperature and pressure conditions, the chemical composition of sulfur compounds contained in the alkaline stream to be regenerated, the type of hydrocarbon sol-=_ vent used, and other factors as will be recognized by those skilled in the art. Based on the improved results utilizing the nitrogen-based promoters, one skilled in the art will know how to adjust these parameters accordingly. Referring now to Fig. 3, there is illustrated a general schematic of a countercurrent liquid-liquid mass transfer appara¬ tus useful in the practice of this invention. The apparatus of Fig. 3 is particularly adapted for the sweetening by catalytic oxidation, sweetening by extraction, and regeneration processes previously described. It should again be noted, however, that the invention herein disclosed and described is not to be limited by its use with the apparatus of Fig. 3 nor is the use of the apparatus of Fig. 3 to be limited to the specific processes herein described. In light of the previous detailed discussion of the sweeten¬ ing and regeneration processes, and in light of the similarity of

operating conditions between the apparatus of Fig. 1 and Fig. 3, the general details of the aforementioned processes and certain specific details of the apparatus need not be described again, and reference may be made to the earlier discussion for such details. For example, the amounts and compositions of the hydro¬ carbon streams, caustic streams, oxidation catalyst, nitrogen- based promoters and the like are similar for both apparatus. Further the fibers of the fiber bundle, operating temperatures and pressures, residence times and the like are also similar for both apparatus. Only those conditions necessary to an under¬ standing of to the operation of the apparatus of Fig. 3 will be mentioned.

The mass transfer apparatus MM of Fig. 3 includes a bundle BB of substantially continuous elongated fibers 82 mounted in a shroud SS and contained within conduit 100. Conduit 100 is provided . with a flange 100a that is adapted for connection or placement with mounting flange 90a of conduit cap assembly 90. A fluid distribution means 120 is mounted within the lower portion of conduit cap assembly 90 for distributing the caustic stream from caustic feed line 80 onto fibers 82 of fiber bundle BB. A fluid gathering means 122 is mounted within the upper portion of conduit cap assembly 90 for gathering the hydrocarbon stream and any entrained caustic stream which has flowed upward through conduit 100 as will be explained below. A fluid outlet line 126 is attached to fluid gathering means 122 for withdrawing the gathered fluids from conduit cap assembly 90. Such gathered

fluids are delivered by fluid outlet line 126 to separator 124, the purpose of which is described below.

Conduit 100 is also provided with a flange 100b which is adapted for placement or connection with mounting flange 110a of collection vessel 110. Collection vessel 110, during the operation of mass transfer apparatus MM, will contain a lower layer 180 of caustic solution and an upper layer 200 of hydrocar¬ bon solution. Shroud SS and fibers 82 of fiber bundle BB extend partly within the confines of collection vessel 110, with the positioning of the downstream end 160 of fiber bundle BB within the caustic solution collected as lower layer 180.

A hydrocarbon feed line 140 is attached to the collection vessel inlet 110b for delivering the hydrocarbon stream into the collection vessel 110. A caustic outlet line 170 is attached to the collection vessel outlet 110c for removing the caustic stream from the collection vessel 110.

Other mechanical details of mass transfer apparatus MM are not necessary to an understanding of the invention, and may be had by referring to the discussion of mass transfer apparatus M of Fig. 1 and the references mentioned therein.

In the operation of the apparatus of Fig. 3, the caustic stream is flowed through caustic feed line 80, into fluid distri¬ bution means 120 and down fiber bundle BB to wet fibers 82. The hydrocarbon stream is simultaneously pumped by pump 128 through collection vessel inlet 110b and into the collection vessel 110 at sufficient pressures and rates so that the hydrocarbon stream

will flow upward through the conduit 100 and thus into contact with the caustic stream wetting fibers 82 of fiber bundle BB.

If mass transfer apparatus MM is being utilized for a cata¬ lytic sweetening process, the caustic stream will generally com- prise a caustic feed having a mercaptan oxidation catalyst therein and the hydrocarbon stream will generally comprise a sour hydrocarbon distillate having an oxidizing agent and the nitrogen-based promoter therein. If mass transfer apparatus MM is being utilized for an extraction sweetening process, the caustic stream will generally comprise only the caustic feed and the hydrocarbon stream will generally comprise only the sour hydrocarbon distillate with the nitrogen-based promoter therein. If mass transfer apparatus MM is being utilized for a regenera¬ tion process, the caustic stream will generally comprise a spent caustic solution having the mercaptan oxidation catalyst therein and the hydrocarbon stream will generally comprise a hydrocarbon solvent having the oxidizing agent and the nitrogen-based promo¬ ter therein.

After contact with the caustic stream, the hydrocarbon stream continues to flow upward through conduit 100 and into conduit cap assembly 90, wherein the hydrocarbon stream and any caustic entrained therein are gathered by fluid gathering means

122, removed from apparatus MM through fluid outlet line 126, then delivered into separator 124. Separator 124 is preferably a gravity separator similar to collection vessel 110 wherein the immiscible caustic and hydrocarbon streams are separated. The

hydrocarbon stream is collected as upper layer 124a and removed from separator 124 through hydrocarbon outlet 190, from which it may be recovered through product line 190 or may be recycled to hydrocarbon feed line 140 for further processing. In the latter event, and under certain conditions as earlier detailed, it may be necessary to pass the hydrocarbon stream through a degassing zone (not pictured) where the pressure is reduced by a suitable pressure relief valve to enable any dissolved gases to come out of solution with the hydrocarbon stream and be separated there¬ from.

The caustic stream is collected as lower layer 124b and recovered from separator 124 through caustic outlet 172 and may be recycled through recycle line 172a to caustic feed line 80 or purged through purge line 172b.

After contact with the hydrocarbon stream in conduit 100, the caustic stream and any hydrocarbon entrained therein continue to flow down fiber bundle BB and into collection vessel 110, wherein the two immiscible streams separate. The hydrocarbon stream accumulates as upper layer 200 where it is recycled through the system. The caustic stream accumulates as lower layer 180 and is withdrawn from collection vessel 110 through collection vessel outlet 110c and into caustic outlet line 170. The caustic stream may then be recovered through caustic product line 170a or may be recycled to caustic inlet line 80 for further processing.

Depending upon the specific process utilized with the appa¬ ratus of Fig. 3, it may be necessary to add fresh caustic and hydrocarbons to the system. Fresh caustic or caustic having the oxidation catalyst therein may be added through caustic feed line ⁵ 70. Fresh hydrocarbon may be added through hydrocarbon feed line 230. If required, oxygen or oxygen—containing gas may be added to the hydrocarbon stream through line 150, and nitrogen-based promoter may be added through line 140a.

The use of the nitrogen-based promoters in conjunction with ° the sweetening and regeneration processes utilizing apparatus MM of -Fig. 3 also significantly increases the efficiency of these processes as indicated by the examples presented hereinafter. The efficiency of these processes will also depend on a number of other parameters such as, for example, the rates of mass trans- 5 fer, the rates of flow of the hydrocarbon and caustic streams, the residence times of the respective streams, the temperatures and pressures at which the processes are operated, the chemical compositions of the sulfur compounds and the hydrocarbon and caustic streams, as well as by the desired mercaptan conversion 0 and other factors as will be recognized by those skilled in the art. Based on the improved results utilizing the nitrogen-based promoters, one skilled in the art will know how to adjust these parameters accordingly.

The foregoing discussion of this invention will be further 5 exemplified by the following specific examples offered by way of illustration and not limitation of the above-described invention.

EXAMPLES

To evaluate the effec iveness of the nitrogen-based promo¬ ters of the present invention, a number of experiments were run. The experiments utilized a procedure called a "shake test" which is defined below. The specific test conditions are provided in each example.

The extraction effects of the nitrogen-based promoters were tested in Examples 1 and 2. In testing the extraction effects, a caustic solution was contacted with a series of hydrocarbon solutions having mercaptans and selected nitrogen-based promoters therein. Equilibrium constants, or q's, were measured to and compared with a base case, that is, a run made without the nitrogen-based promoter, to determine the effects of the promo¬ ters on the ability of the mercaptans to transfer from the hydro¬ carbon phase to the caustic phase.

The catalytic oxidation effects of the nitrogen-based promo¬ ters were tested in Examples 3 through 8. In testing the cataly¬ tic oxidation effects, a caustic solution having a mercaptan oxidation catalyst therein was contacted with a series of hydro¬ carbon solutions having- mercaptans and selected nitrogen-based promoters therein. The mercaptan concentrations of the resulting hydrocarbon products were measured and compared with a base case to determine the effectiveness of the promoters on the oxidation reaction.

The color effects of the nitrogen-based promoters on selec¬ ted of the resulting products were tested in Examples 9 and 10.

Accelerated color tests were performed on the products and the Saybolt colors measured to determine any color changes caused by the use of the promoters.

The following terms are defined for the purposes of these Examples:

(a) "Shake test" refers to a simplified procedure utilized in determining the extraction and catalytic oxidation effects of the nitrogen-based promoters of this invention. The general "shake test" procedure is as follows, with the specific operating parameters defined in each Example:

(1) a sodium hydroxide solution of the desired concentra¬ tion is prepared;

(2) the desired amount and type of mercaptan oxidation catalyst is added to the sodium hydroxide solution (for strict extraction tests, this step is omitted);

(3) 100 ml of a hydrocarbon is added to a 150 ml separatory funnel;

(4) the separatory funnel is placed in an oven and heated to the desired temperature;

(5) the desired amount and type of nitrogen-based promoter is added to the heated hydrocarbon (for the base cases, this step is omitted) ;

(6) the desired amount of sodium hydroxide solution (with or without oxidation catalyst) is added to the heated hydrocar¬ bon;

(7) the contents of the separatory funnel are shaken for a desired time and allowed to settle for about 15 minutes; and

(8) samples of the hydrocarbon and sodium hydroxide phases are withdrawn and analyzed for mercaptan concentration in accor¬ dance with ASTM D3227-73.

As previously mentioned, the specific experimental condi¬ tions are given in each example, which may include omitting certain steps, most particularly steps 2 and 5.

(b) "Mixed Nitrogens" refers to a nitrogen stream produced as a by-product from the processing of coal tars. The exact composition of the stream is unknown and may vary, but it is comprised primarily of pyridine, indole, aniline, quinoline and isoquinoline based compounds.

(c) "Accelerated Color Tests" were conducted in accordance with ASTM Dl56-64.

(d) "Kq" refers to an equilibrium constant measured to determine the effects of the promoters on the ability of the mercaptans to transfer from the hydrocarbon phase to the caustic phase. "Kq" is calculated by dividing the concentration of mercaptan compounds in the caustic phase by the concentration of mercaptan compounds in the hydrocarbon phase.

Example JL, A kerosene comprising approximately _^ 9^il _^ ppji _^ of__ _. me-rcapta ^f ' was contacte 'with a 20% NaOH solution at ambient temperature and pressure. The volumetric ratio of the hydrocarbon to NaOH solu¬ tion was 5:1. No mercaptan oxidation catalyst was added. The

two solutions were shaken for one minute, at which time the phases were separated and the mercaptan level in each phase measured.

As the results show, the addition of nitrogen-based .promo- ^J ters to the system signi icantly increased the mercaptan concentrations in the NaOH solution and, therefore, significantly increased the Kq values. This clearly indicates that the addi¬ tion of the promoters has a significant positive effect on the extraction of mercaptan compounds from hydrocarbon streams.

5

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TABLE I

Mercaptan

Concentration

(ppm)

Nitrogen Promoter Feed Product Caustic Kq's Material Balance (%)

Base (No Promoter) 950 849 389 .46 98 5 ppm pyridine 950 666 1513 2.3 102 5 ppm pyrimidine 950 583 1737 3.0 98 5 ppm aniline 950 687 1482 2.15 104 5 ppm quinoline 950 693 1439 2.1 103 5 ppm melanine 950 718 1043 1.5 98

Example 2 A kerosene comprising approximately 1060 ppm of mercaptans was again contacted with a 20% NaOH solution at ambient tempera¬ ture and pressure conditions. The volumetric ratio of the hydro- carbon to the NaOH solution was again 5:1, and no mercaptan oxidation catalyst was added. The two solutions were shaken for one minute, the phases were separated, then the mercaptan concen¬ tration in each phase measured. The results are presented in Table II.

As can be seen from the results, the addition of the nitrogen-based promoters again significantly increased the Kq values over the base case. One additional phenomena to be noted is that the use of larger amounts of the promoters may actually have less effect than the optimal smaller amounts . This is evidenced by the decreased Kq values when 10 ppm and 100 ppm of pyridine are added versus the addition of 5 ppm.

TABLE II

Mercaptan

Concentration

(ppm)

Nitrogen Promoter Feed Product Caustic Kq's

Base (No Promoter) 1060 949 463 .49

Pyridine (5 ppm) 1060 666 1513 2.3

Mixed (5 ppm) Nitrogens 1060 671 1497 2.2

Pyrimidine (5 ppmj 1060 583 1737 3.0

Pyridine (10 ppm) 1060 660 1487 2.25

Pyridine (100 ppm) 1060 700 1282 1.83

Example 3_ A kerosene comprising approximately 950 ppm of mercaptans was contacted with a 20% NaOH solution having 200 ppm cobalt phthalocyanine catalyst therein in a series of one minute shake tests. The volumetric ratio of the kerosene to NaOH solution was 5:1, and the two were contacted in the presence of well over the stoichiometric amount of oxygen at a temperature of 150°F and ambient pressure. The effect of the addition of each of a varie¬ ty of nitrogen-based promoters to the above described system was tested.

The results of the tests are provided in Table III and clearly show improved mercaptan conversion. As can be seen, the use of the nitrogen-based promoters signi icantly reduced the mercaptan levels in the product streams. The results, therefore, provide a strong indication of the positive effects of using the nitrogen-based promoters in the practice of this invention.

TABLE III

Mercaptan Concentration

Nitrogen (ppm)

Additional Additional

Promoter One Minute One Minute One Minute

- Feed Product Feed Product Feed Product

Base (No Promoter) 950 301 301 273 - -

Pyridine (5 ppm) 950 190 190 70 - -

Pyrimidine (5 ppm) 950 80 80 10 - -

Pyrimidine (1)

(5 ppm) 950 51 51 0 — —

Aniline (5 ppm) 950 187 187 130 - -

Quinoline (5 ppm) 950 191 191 122 - -

Melamine (5 ppm) 950 ^" 273 273 199 - -

Mixed Nitrogens

(5 ppm) 950 125 125 98 98 87

(1) Temperature increased to 170° F.

Example 4. A gasoline condensate stream from a gas well comprising approximately 118 ppm mercaptans was contacted with a 15% NaOH solution having 200 ppm cobalt phthalocyanine disulfonate cata- lyst therein in a series of one minute shake tests. The volume¬ tric ratio of the gasoline to NaOH solution was 5:1, and the two were contacted in the presence of well over the stoichiometric amount of oxygen at a temperature of about 100° F and at ambient pressure. The effect of the addition of each of a variety of nitrogen-based promoters to the above described system was tes¬ ted.

The results of the tests are provided in Table IV. As can be seen, the results clearly show improved mercaptan conversion and provide a strong indication of the effectiveness of using the nitrogen-based promoters in the practice of this invention.

TABLE IV

Mercaptan Concentration

Nitrogen (ppm)

Additional Additional

Promoter One Minute One Minute One Minute Feed Product NaOH Feed Product NaOH Feed Product NaOH

Base (No

Promoter) 118 30 0 30 19 19 18

Aniline (5 ppm) 118 8 0

Pyridine (5 ppm)118 9 0

Example |>

Another gasoline stream comprising approximately 290 ppm mercaptans was contacted with a 15% NaOH solution having 200 ppm cobalt phthalocyanine disulfonate catalyst therein in one minute standard shake tests. The volumetric ratio of the gasoline to the NaOH solution was 5:1, and the two were contacted in the presence of well over the stoichiometric amount of oxygen at a temperature of 100°F and at ambient pressure. The effect of the addition of each of a variety of nitrogen-based promoters to the above described system was again tested.

The results of the tests are provided in Table V. As can again be seen, the results clearly show improved mercaptan con¬ version and provide a strong indication of the ef ectiveness of using the nitrogen-based promoters in the practice of this inven¬ tion.

TABLE V

Mercaptan Concentration (ppm)

Nitrogen Promoter

Feed Product NaOH

Base (No Promoter) 290 23 0 Pyridine (5 ppm) 290 0 0 Aniline (5 ppm) 290 0 0 Pyrimidine (5 ppm) 290 0 0 Mixed Nitrogens (5 ppm) 290 0 0

Example 6_

A gasoline having approximately 320 ppm of mercaptans there¬ in was contacted with a 15% NaOH solution having 200 ppm cobalt phthalocyanine disulfonate catalyst therein in a series of thirty second and one minute standard shake tests. The volumetric ratio of the gasoline to NaOH solution was 5:1, and the two were con¬ tacted in the presence of well over the stoichiometric amount of oxygen at a temperature of 100°F and ambient pressure. The effect of the addition of a variety of nitrogen-based promoters to the above described system was tested.

The results of the tests are provided in Table VI and clear¬ ly show the positive effects of adding the nitrogen—based promo¬ ters to the system.

TABLE VI

Mercaptan Concentration (ppm)

Nitrogen

Additional Promoter Thirty Seconds Thirty Seconds One Minute

(1)

Feed Product NaOH Feed Product NaOH Feed Product NaOH

Base (No 320 100 100 30 Promoter)

Base (No 320 40 Promoter)

Pyridine (5 ppm) 320 66 66 19 Pyridine (5 ppm) ^• 320 20

Methenaraine (5 ppm) 320 54 54

Methenamine (5 ppm) 320 10

Fresh NaOH solutions were used in the additional thirty second period.

Example 7 A kerosene comprising approximately 1000 ppm of mercaptans was contacted with a 20% NaOH solution having 200 ppm cobalt phthalocyanine disulfonate catalyst therein in a series of one minute standard shake tests. The volumetric ratio of the kero¬ sene to NaOH solution was 5:1, and the two were contacted in the presence of well over the stoichiometric amount of oxygen at a temperature of 150°F and ambient pressure. The effects of the addition of 5 ppm of each of a wide variety of nitrogen-based promoters to the above described system was tested.

The results of the tests are provided in Table VII. As can be seen from the results, all of the listed nitrogen compounds enhance the conversion of the mercaptans over the base case without the promoter. After one minute, only 64% of the mercap¬ tans in the base case were converted while anywhere from 80% to 93% of the mercaptans were converted utilizing the promoters. After two minutes, only 82% of the mercaptans in the base case were converted while anywhere from 84% to 99% of the mercaptans were converted utilizing the promoters. These results clearly indicate that the use of nitrogen-based promoters has positive effects on the processes utilized in the practice of this inven¬ tion.

Those compounds found to be especially preferred include 1- phenylpyrrole, pyradazine, pyrimidine, methylpyrimidine, methen¬ amine, 3-aminoquinoline, 5-triazolo [4,3-a] quioline, 4-azabenzi- midazole, pyridopyrazine, 1,3,5 triazine, benzotriazole (Sandoz) ,

pyrazine, 2-aminopyrimidine, 4-methyl piperidine, piperidine, azabicyclo [3,2,2] nonane, and 2,4 diaminotoluene.

TABLE VII

Mercaptan

Concentration

Nitrogen (ppm) % Conversion

Additional Additional Promoter One Minute One Minute One Minute One Minute

Base (No Promoter) 360 180 64 82

Pyridine 192 130 81 87

Picoline 189 158 81 84

Nicotinonitrile 151 97 85 90

1-Phenyl Pyrrole 107 47 89 95

Phenazine 110 60 89 94

Pyradazine 85 22 92 98

Pyrimidine 85 10 92 99

2,2 Bipyridine 131 101 87 90

Quinoline 191 122 81 88

Methyl Pyrimidine 96 55 90 95

Mixed Nitrogens 125 100 88 90

Methenamine 91 44 91 96

3,4 Diamino Pyridine 126 107 87 89

Acridine 118 74 88 93

Quinaldine 167 127 83 87

NINl-Dimethyl

Benzylamine 110 65 89 93 Isoquinoline 117 120 83 88 4—Aminopyrazolo [3,4-d] Pyrimidine 131 85 87 92 3 Aminoquinoline 97 38 90 96 7—Azaindole 126 87 87 91 S-Triazolo [4,3-a]

Quinoline 99 53 90 95 4-Azabenzimidazole 87 29 91 97 Pyrido Pyrazine 98 33 90 97 Amino Piperidine 121 70 88 93 1,3,5 Triazine 91 55 90 95 L Histidine 114 89 89 91 2,2 Biquinoline 142 ■111 86 89 Benzotriazole (Sandoz) 83 42 92 96 Quinoxaline 115 101 88 90 1,2,4 Triazole 125 92 87 91 5-Aminoindazole 131 112 87 89 Triethylene Diamine 107 94 89 91 Aminopyrazole 177 149- 82 85 5,10,15,20 Tetraphenyl-

21H,23H Porphine 100 75 90 93 Pyrazine 80 55 92 95

TABLE VII (continued)

Nicotine 195 112 85 89

2-Anilinopyridine 121 97 88 90

2-Aminopyrimidine 91 30 91 97

4-Dimethyl Amino

Pyridine 106 86 89 91

Benzimidazole (Archem) 112 86 89 91

N,Methyl Tolyimidazole

(Archem) 103 78 90 92

Tolyimidazole (Archem) 104 83 90 92

Pyrrole 203 158 80 84

Pyrrolidine 181 149 82 85

4 Methyl Piperidine 111 50 89 95

2,5 Dimethyl Pyrrole 191 157 81 84

Piperidine 73 42 93 96

Piperazine 123 68 88 93

Pyrazole 137 82 86 92

Indole 152 119 85 88

5 Methyl Indole 197 . 149 80 85

Indoline 149 • 112 85 89

Polyvinyl Piperidine 163 128 84 87

Skatole .107 60 89 94

Azabicyclo [3,2,2]

Nonane 103 44 90 96

4-Aminopyrene 107 63 89 94

Phthalocyanine 140 119 86 88

Homopiperazine 117 87 88 91

1,4,8,12 Tetra- azacyclopentadecane 110 93 89 91

5-Amino Indole 112 84 89 92

Carbazole 110 80 89 92

Aniline 187 130 81 87

2,5 Dimethyl Aniline 190 142 81 86

2,4 Diamino Toluene 99 39 90 96

Toluidine 138 118 86 88

Methylamine 129 109 87 89

Cycloxexylamine 119 101 88 90

Urea 272 150 83 85

T-Octylamine 167 120 83 88

Octadecylamine 146 100 85 90

Ethylenediamine 157 119 84 88

L-Isoleucine 102 71 90 93

Triethylene Tetramine 132 110 87 89

Butylamine 117 103 88 90

Tolunitrile 158 111 84 89

Nitrobenzene 129 115 87 88

N-Heptylcyanide 166 142 83 86

Example 8_

A kerosene comprising approximately 1000 ppm of mercaptans was contacted with a 20% NaOH solution having a varying amount of a carboxylated cobalt phthalocyanine catalyst therein in a series of one minute shake tests. The volumetric ratio of the kerosene to NaOH solution was 5:1, and the two were contacted in the presence of well over the stoichiometric amount of oxygen at a temperature of about 150°F. and at ambient pressure. The effect of utilizing various amounts of a carboxylated catalyst instead of the sulfonated catalyst was tested.

The results of the tests are provided in Table VIII. As can be seen, the nitrogen-based promoters enhance the conversion of the carboxylated catalyst at all concentrations. These results again show the effectiveness of using the nitrogen-based promo¬ ters in the practice of this invention.

TABLE VIII

Mercaptan Concentration % Conversion

Catalyst Nitrogen (ppm) Concentration (ppm) Promoter

Additional Additional

One Minute One Minute One Minute One Minute

Product NaOH Product NaOH

50 Base (No 417 47 308 46 58 69 Promoter)

50 Methenamine 160 33 90 35 83 91 (5 ppm)

50 Mixed Nitrogen 177 34 143 37 82 86 (5 ppm)

100 Base (No 411 ^' 32 308 39 59 69 Promoter)

100 Methenamine 152 30 88 27 85 91 (5 ppm)

100 Mixed Nitrogen 170 28 143 27 83 86 (5 ppm)

150 Base (No 407 7 193 7 59 81 Promoter)

150 Methenamine 150 81 85 92 (5 ppm)

150 Mixed Nitrogen 163 10 140 84 86 (5 ppm)

200 Base (No 406 193 59 81 Promoter)

200 Methenamine 150 74 85 93 (5 ppm)

200 Mixed Nitrogen 160 137 84 86

Example 9 An accelerated color test was run on the kerosene feed and several of the products from Example 3. The results, presented in Table IX, indicate that the presence of small amounts of the nitrogen-based promoters in the hydrocarbon product had little, if any, detrimental effect of the product color properties.

TABLE VIX

Saybolt

Color

Nitrogen

Hydrocarbon

Before After

Promoter

Heat Heat

Feed None +29 28

Product None +29 28

Product Pyridine (5 ppm) +29 28

Product Pyrimidine (5 ppm) +29 28

Product Aniline (5 ppm) +29 28

Product Quinoline (5 ppm) +29 28

Example 10 Another accelerated color test was run on the gasoline feed and some of the products from Example 6. The results, presented in Table X, indicate that the presence of the nitrogen-based promoter does have an effect on the color properties of the gasoline, as to be expected; however, the small amounts of nitrogen-based promoters used in Example 6 only cause a minimal decrease in the Saybolt Color, with the resulting color being well within the normal gasoline specification of 25.

TABLE X

Saybolt Color

Nitrogen

Hydrocarbon

Before After - Promoter Heat Heat

Feed None 30 28

Product None 30 28

Product Pyridine (5 ppm) 30 26

Product Methenamine (5 ppm) 30 26

Those skilled in the art will be able to make variations of this invention from the foregoing descriptions and examples with¬ out departing from the scope and spirit of the claimed invention.