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Publication numberUS2769757 A
Publication typeGrant
Publication dateNov 6, 1956
Filing dateJul 26, 1954
Priority dateJul 26, 1954
Publication numberUS 2769757 A, US 2769757A, US-A-2769757, US2769757 A, US2769757A
InventorsWeldon G Annable, Robert M Haines
Original AssigneePure Oil Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Preparation of non-corrosive naphthas by reacting refined naphtha with barium molybdate or zinc molybdate
US 2769757 A
Abstract  available in
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Description  (OCR text may contain errors)

United States Patent PREPARATION OF NON-CORROSIVE NAPHTHAS BY REACTING REFINED NAPHTHA WITH BARIUM MOLYBDATE R ZINC MOLYBDATE Weldon G. Annable, Mundelein, and Robert M. I-Iaines, Crystal Lake, Ill., assignors to The Pure Oil Company, Chicago, ]1l., a corporation of Ohio No Drawing. Application July 26, 1954, Serial No. 445,929

4 Claims. (Cl. 196-28) This invention is directed to a method for the production of petroleum naphthas characterized by their ability to pass the distillation-corrosion test and, more particularly, the invention relates to the production of noncorrosive naphtha hydrocarbons by chemical reaction or treatment at a temperature of about 400 to 500 F.

Crude petroleum has long been the source of widely known products including gasoline, kerosine, diesel fuels, lubricating oils, and heavy tars. In many instances, the products obtained from petroleum are employed as reactants in the synthesis of additional petroleum derivatives and chemicals and a large number of products of petroleum are used directly without extended treatment or modification. Petroleum naphthas comprise a wide variety of such latter products used extensively in the dyeing, rubber, extraction, protective coating, and allied industries. A large portion of the petroleum naphthas used is the straight-run naphthas which are selected frac tions of the lower boiling, more volatile constituents of crude petroleum. The present invention is directed to a method of transforming deleterious sulfur compounds present in hydrocarbon mixtures into forms which are less obnoxious and non-corrosive and will be illustrated by the treatment of straight-run naphthas. The examples given are not to be construed as limiting the invention. The term naphthas as herein used shall mean straightrun petroleum naphthas and other hydrocarbon mixtures or their equivalents containing deleterious sulfur compounds which must be transformed to meet rigid corrosion tests.

Naphthas prepared from petroleum by physical means inevitably contain other types of organic and inorganic compounds due to the complex nature of petroleum which are deleterious as far as certain end uses of the naphthas are concerned and necessitate the application of additional refining steps. Even with such additional refining, it is exceedingly diflicult to prepare naphthas which meet the exacting specifications that have been established by the industry. Of these deleterious non-hydrocarbon compounds, the sulfur and sulfur-containing constituents are generally the most persistent and cling tenaciously to any environment in which they exist, imparting objectionable odor, corrosiveness, color, and other physical and chemical properties thereto. The odor of naphthas is important; however, no standard test exists to cover this property and the odor of a well refined naphtha is generally described as sweet.

I Tests have been devised to determine both quantitatively and qualitatively the presence of these odious compounds in an attempt to control the properties and quali'ty of naphthas from petroleum sources. For this pur- "ice pose, various copper strip corrosion tests, the mercury test, the lead acetate test, and the doctor test are used. Procedures established by A. S. T. M. are used to determine the content and distribution of these sulfur compounds. Perhaps the most critical and rigorous qualitative test for determining the presence of corrosive sulfur compounds in naphthas is the distillation-corrosion test, known also as the Philadelphia test, the Amsco corrosion test, or the full boiling range corrosion testby any name, a particularly rigorous species of copper strip corrosion test. The test, widely applied by the manufacturers, distributors, and users of specialty naphthas, is carried out by the addition of a small pure copper coupon to an ordinary A. S. T. M. distillation flask containing cc. of the naphtha to be tested. The copper strip is so positioned in the flask that one end of the strip contacts the residue at the end of the distillation, and the distillation is conducted according to A. S. T. M. D86-38 as described in A. S. T. M. Standards on Petro-' leum Products and Lubricants, published by the American Society for Testing Materials, Philadelphia, Pennsylvania.

At the completion of the test, wherein the flask has been heated to dryness, the color of the copper strip is an indication of the relative amount of corrosive sulfur compounds present in the naphtha sample. A negative test is shown by the presence of a very slight or moderate tarnish on the strip and stamps the naphtha as satisfactory. If the copper strip becomes moderately blackened, the results are interpreted as positive or unsatisfactory. The production of a slightly tarnished or slightly colored or corroded strip, indicated by a dark orange with peacock colorations thereon, is termed borderline and as such denotes a naphtha which is not acceptable and must be further refined. The market is limited for off-specification naphthas and further refining is expensive since even then there is no assurance that the product will pass the severe distillation-corrosion test.

The subjection of high sulfur content naphthas to various refining and sweetening operations which may include oxidation and extraction methods, or the recycling of rejected off-specification naphthas back through such a process, does not produce acceptable naphthas because the sulfur compounds remaining are the most difficult to remove and the most corrosive. High sulfur content naphthas usually have a poor odor as Well as other undesirable properties. If straight-run naphthas from high sulfur crudes are subjected to other more severe refining methods, the resulting products may pass the other tests for sulfur compounds but do not pass the distillation-corrosion test. Often naphthas are produced which are negative or borderline to the distillation-corrosion test and which exhibit a positive reaction to one or more of the other tests for sulfur compounds. Since naphthas must pass all such tests to be acceptable, further treatment is necessary. Prior art methods of desulfurization when applied to such naphthas may produce a doctor negative or mercury negative product, but in so doing the end result is a positive distillation-corrosion test.

Accordingly, the primary object of this invention is to overcome this problem and provide a process for producing improved naphthas by chemical reaction or treatment F. and preferably at 450 F.

A second object of the invention is to provide a method of producing naphthas which pass the distillation-corrosion test from naphthas containing unacceptable amounts of sulfur compounds.

These and other objects of the invention will become apparent as the description thereof proceeds.

In the prior art there are described many methods for desulfurizing and sweetening hydrocarbon mixtures. These processes may be roughly divided into two groupsthose involving chemical treatment or adsorptive contact .at low temperatures with the main purpose being the removal of free sulfur, hydrogen sulfide, and those organic sulfur compounds which may be adsorbed; the second group of processes, which include hydrodesulfurization reactions, are conducted at elevated temperatures and involve the breakdown of the organic sulfur compounds into products including hydrogen sulfide. During these hydrodesulfurization processes, the sulfur compounds present are substantially completely transformed and there takes place reactions involving hydrogenation, dehydrogenation, reforming, and the like, depending on the particular catalyst used and the operation conditions. In general, especially in the presence of hydrogen under optimum conditions, gasoline products are obtained which have increased octane numbers and good lead susceptibility. Products produced by these methods have their sulfur contents greatly reduced, and it is not uncommon to reduce the sulfur content to points below 0.01 percent sulfur. These prior art processes cannot be depended upon to produce naphthas which are non-corrosive to the distillation-corrosion test because the types of organic sulfur compounds remaining after these treatments are the very types that are corrosive to copper and, though present in a very small amount, are deleterious and indicate an unsalable product. Therefore, a sharp distinction must be made between desulfurization generally as meant in the prior art and the desulfurization necessary to produce noncorrosive naphthas. The present invention is directed to the finding that at a temperature of about 400 to 500 F. zinc molybdate and barium molybdate may be used to contact naphtha hydrocarbons to transform the sulfur compounds therein to forms which are non-corrosive to the distillation-corrosion test. It has been found that at temperatures below 400' F., although there may be a large degree of desulfurization, the remaining sulfur compounds are corrosive to the distillation-corrosion test. In ordinary gasoline sweetening processes using oxidizing agent, the general object is to convert the mercaptans to disulfides. At temperatures above about 350 F., the disulfides break down and form lesser amounts of corrosive sulfur compounds. Thus, because of the instability of the disulfides, these methods of desulfurization or sweetening cannot be used to produce sweet naphthas. This is especially true in considering crude naphthas which have above about 0.003 percent mercaptans. If the chemical treatment or desulfurization is carried out according to the prior art at temperatures of above 500 F., there may be adequate desulfurization, but by-products are formed at these elevated temperatures which deleteriously affect the color of the resultant naphthas. This color cannot be removed by ordinary adsorbents, and again the product is unsalable.

It has been found that at a temperature of about or above 400 F. some of the mercaptans are converted to metal mercaptides instead of disulfides and as the temperature is maintained, or raised to about 450 F. the metal mercaptides break down into metal sulfides and organic monosulfides which are non-corrosive and stable. This is the type of sweetening reaction which is contemplated by the present invention. There is no minimum sulfur content requirement for naphthas but, since they must meet the doctor test, contains no hydrogen sulfide or free sulfur, and pass the distillation-corrosion test, the amount of total sulfur present in the r 4 finished product is necessarily small. The principal factors pertaining to the influences exerted by this small content of sulfur compounds on the various corrosion tests are the boiling points of the sulfur compounds in relation to the boiling range and end point of the naphtha, and the stability of the sulfur compounds at moderately high temperatures. Mercaptans are rather unstable at moderately high temperature and break down into products corrosive to the distillation-c0rrosion test. Disulfides are more unstable and produce very corrosive decomposition products, especially under the conditions present in the distillation residue. High boiling naphthas like Stoddard solvent generally give a more corroded copper strip than lower boiling naphthas, as rubber solvent. Treatment of off-specification naphthas by prior art methods may break down the sulfur compounds into those types which are more corrosive :to the distillation-corrosion test, especially where low sulfur naphthas are concerned since these sulfur compounds are most difficult to remove and most corrosive.

Accordingly, the present invention is primarily directed to the treatment of naphthas or hydrocarbon mixtures containing sulfur contents in the order of about 0.16 percent by weight or less of total sulfur. The total sulfur may comprise elemental sulfur or sulfur compounds or mixtures of sulfur and one or more types of sulfur compounds. Crude naphthas having more than this amount of total sulfur may be treated in accordance with the invention but it is preferred that such naphthas be previouslydesulfurized to bring the sulfur content down to 0.16% or to as low as 0.025 percent or less total sulfur. The 0.025 percent total sulfur may be mercaptan sulfur only and one embodiment of the invention comprises the treatment of naphthas containing substantially only mercaptan sulfur compounds. The chemical treatment with zinc molybdate and barium molybdate at 400 to 500 F., in combination with prior desulfurization as described in accordance with this invention, may effect a considerable reduction in the total sulfur content of the naphthas, as by as much as percent, but generally the reaction is one of sweetening or transformation of the sulfur compounds into non-corrosive form.

The following illustrative examples exemplify the instant process.

EXAMPLE I A sour, corrosive, Texas naphtha containing 0.163% total sulfur was passed through a treating agent, consisting of zinc molybdate supported on alumina, at 450 F., substantially atmospheric pressure, and a space velocity of about one. Analyses of the corrosive naphtha charged and the non-corrosive naphtha produced were as follows:

Table I THE PRODUCTION OF NON-CORROSIVE NAPHTHAS USING ZINC MOLYBDATE EXAMPLE II A sample of the same sour, corrosive, Texas naphtha containing 0.163% total sulfur processed the same as Example I was treated under the same operation employing barium molybdate supported on alumina. Analyses of the corrosive naphtha charged and the noncorrosive naphtha produced were as follows:

Table II THE PRODUCTION OF NON-CORROSIVE ENAPHTHAS USING BARIUM MOLYBDATE The product was of good color and odor and was noncorrosive when subjected to the critical distillation-corrosion test. The products from this treatment may be fractionated into the various specialty naphthas desired.

Although the invention in its broadest aspects is not to be limited to the treatment of hydrocarbons containing any particular amount or kind of sulfur compounds, some explanation of the relationship of sulfur content and severity of treatment is in order. As previously explained, prior art high temperature desulfurization processes, although greatly reducing the sulfur contents of the products, leave therein those types of sulfur compounds which give a positive distillation-corrosion test.

Naphthas containing about 0.16 weight percent sulfur are considered to be high sulfur naphthas which are ordinarily difficult to desulfurize by prior art methods. By maintaining the temperature at between about 400- 500 F. using zinc molybdate and barium molybdate as the treating material, no hydrogen sulfide will appear in the product and a successful treatment is obtained. This is also true of the hydrocarbon mixtures containing greater amounts of sulfur provided the teachings of this invention are followed. Thus by treating a fraction containing as much as 2.0% of sulfur if the temperature does not exceed 500 F., no hydrogen sulfide will appear and a non-corrosive product will be formed. In those instances where hydrogen sulfide is formed, the reaction must be terminated before hydrogen sulfide appears, otherwise a product exhibiting a negative distillationcorrosion test cannot be obtained. If temperatures above 500 F. and as high as 750 F. are used, successful treatment is impossible not only because of the appearance of hydrogen sulfide which forms corrosive sulfur compounds in the products, but because of the general nature of the remaining sulfur compounds, especially a small amount of mercaptans inevitably present. Thus even if the prior art methods of desulfurization at temperatures above 500 F. wherein the reaction is terminated before the appearance of a substantial amount of hydrogen sulfide in the products are used, the results of this invention will not be obtained.

In order to further demonstrate the invention, the following table is shown wherein various treating agents were investigated as to their ability to transform the corrosive sulfur compounds in a naphtha to non-corrosive forms as evidenced by a good or bad distillationcorrosion test. In these tests, the same West Texas naphtha was used as in the previous experiments and the same reaction conditions were used, with the exception that in run No. 22 using iron molybdate the supporting material was Aloxite. In this run the total sulfur was reduced from 0.158 weight percent to 0.144 weight percent. The product was sour and corrosive. Sulfur. distribution tests in those materials which were unsatisfactory as far as the distillation-corrosion test is concerned were not run. In each instance, with the exception of copper nitrate, the materials used gave a product of good color. The table shows whether or not there has been a reduction in sulfur content and whether or not the product passedthe distillation-corrosion test.


Good Dis- Desulfurtillatlonizatlon Corrosion Test . Copper chloride Active carbon 10. Porocel (regenerated) 11. Fullers earth 3. No. 4. Yes 5. Yes 6. Copper oxalate N0. 7. Copper nitrate No. 8

12. Filtrol X-417. No. 13. Filtrol X-466. No. 14 Nickel vanadatc No.

15. Sea Sorb (MgO) 16. Ammonium molybdate. 17. Borax glass 18. Sodium bicarbonate 19. Lithium carbonate- 20. Molybdenum oxide.-. 21 Vanadium pentoxide- 22. Chromic oxide 23. Iron molybdate Yes Yes In practicing the present invention, any hydrocarbon material from which naphthas or solvents or similar products may be obtained can be used and subjected to treatment with zinc molybdate and barium molybdate at 400 to 500 F. wherein the objective is to overcome the tendency of the product toward the formation of carryover of those types of sulfur compounds which cause a positive distillation-corrosion test. Fractionation into various specialty naphthas may precede or follow treatment in accordance with the invention. Although the present process may be applied to products boiling up to 700 F. with adequate results as far as desulfurization is concerned, for those materials boiling over 400 F. the distillation-corrosion test is not applied and only those products boiling under 400 F. must meet this severe test. Products boiling above 400 F. must pass the less severe immersion corrosion tests. Accordingly, to prolong the life of the treating agents, it is preferred that the more volatile components and the high boiling residues or products boiling above about 400 F. that are present he removed by fractionation or other methods prior to treatment in accordance with the invention. As another example, a crude oil containing from 1.0 to 3.0 or as high as 7.0 weight percent of sulfur may be fractionated to obtain a wide boiling range virgin or straightrun naphtha having an end boiling point of about 500 P. which may be treated in accordance with the invention. A gas oil fraction may be used which may boil between about 500 and 700 F. Kerosine fractions may also be used. Preferably a straight-run naphtha fraction having up to 0.16 percent of total sulfur and boiling between 110 and 450 F. or a previously desulfurized fraction having 0.05 percent sulfur, especially as mercaptan sulfur, is treated in accordance with this invention.

The boiling range of the particular fraction removed for treatment or after treatment in accordance with this invention may be varied somewhat from the boiling ranges given depending upon the relative amounts of specialty naphtha, rubber solvent, V. M. & P. naphthas desired. By narrowing the boiling range of the virgin naphtha to within to 250 F., the process may be directed to obtaining rubber solvents almost exclusively. On the other hand, by starting with a fraction boiling between 200 and 400 F., the process may be directed to production of V. M. & P. solvents and specialty naphthas. In one specific embodiment of the invention, the treatment of the entire first fraction boiling up to 500 F. or more to produce a wide variety of products ranging from rubber solvents up to high boiling specialty naphthas including, for example, petroleumether 90 140 F., Special Textile Spirits 180,210 E, Light Mineral Spirits 290330 F., Stoddard Solvent 310385 F., and High Flash Dry Cleaning Solvent 360400 F.,lal1 being non-corrosive, odorless, and meeting the rigorous requirements of the industry, is contemplated.

In treating naphtha fractions or hydrocarbon mixtures from which naphtha fractions may be separated, which contain above 0.16 percent sulfur, as, for example, a naphthacontaining from 0.20 to as high as 7.0 percent total sulfur, it is desirable to subject the naphtha to a desulfurization reaction before treatment in accordance with the invention. For this purpose, the naphtha may be vaporized and passed over a bauxite catalyst at 700 to 800 F. A hydrodesulfurization reaction may be employed if the naphtha contains a considerable portion of sulfur compounds. Treatment with such desulfurization catalysts as molybdates, sulfides, and oxides of iron group metals and mixtures, including cobalt molybdate, chromic oxide, vanadium oxide with molybdena and alumina, and sulfides'of tungsten, chromium of uranium, with or without thepresence of hydrogen at temperatures from 500 F. to 800 F. and under pressures from 20 to 500 pounds per square inch will elfectively desulfurize the naphthas as a pretreatment.

Although preferred treating conditions for low sulfur naphthas are temperatures of about 450 F., pressures approximately atmospheric, and space velocities around 1.0, operation in general may be'carried out at temperatures between about 400 and 500 F., superor subatmospheric pressures, and space velocities between about 0.2 and 10. The term space velocity as used herein may be defined as the liquid volumes of feed per unit of time per unit volume of reactor. In another variation of the process to produce non-corrosive naphthas by treatment with zinc molybdate and barium molybdate, treatment under the less severe conditions also may be used as the second step of an over-all process wherein the first step is a desulfurization carried out with either zinc or barium molybdate as the catalyst or with a different catalyst, as mentioned above, known for the purpose. The preferred treating agent is co-precipitated zinc molybdate and alumina, and may be regenerated by heating at temperatures between 900 and 1500 F. to reduce the sulfur content to below 1 percent.

In certain instances, it may be desirable to increase the solvency of the naphthas produced. For this purpose, the naphthas may be first subjected to a mild reforming or hydroreforming operation preceding the chemical treatment with zinc or barium molybdate. The hydroreforming may be conducted using a cobalt molybdate or copper molybdate catalyst and the sour naphtha passed thereover at temperatures between 825 and 850 F. The aromatization may be promoted by a platinumcontaining catalyst at 800 to 825 F. Since these processes of desulfurization and aromatization are well known and merely used as preliminary treatments for the present process, further description is unnecessary.

In carrying out the reaction, the naphtha to be treated is heated to a temperature of about 400 to 500 F. and preferably 450 F. and the vapors passed through the zinc and barium treating agents. Adequate conversion of the sulfur compounds to non-corrosive form may be obtained by passing the hot liquid naphtha under pressure through the zinc and barium treating agents. The vapor treatment is preferred because of the ease with which the reaction may be carried out. Space velocities of from 0.2 to 10 may be used. Any of the well known percolation, fixed bed, fluidized reaction zone, or plural bed vapor-solid contact methods of the prior art may be used as long as intimate contact is obtained at a temperature within 400 to 500 F. Since the degree of treatment depends somewhat on the correlation between temperature and time of contact as in all such chemical transformations, it is usually desirable to conduct the treatment at relatively high space velocities when temperatures above 450 F are used and at lower space velocities when temperatures below 450 F. are used. In general, the space velocity is selected to give results corresponding to those obtained at a vapor space velocity in the range of about 0.2 to 3.0 at 20 pounds per square inch pressure at about 450 F. These conditions consistently give satisfactory results.

Zinc molybdate and barium molybdate are available commercially or may be prepared from raw materials. Zinc molybdate and barium molybdate may be formed by reaction of a water-soluble zinc or barium salt, such as zinc or barium nitrate, zinc or barium acetate, zinc or barium salicylate, zinc or barium fluoride, zinc or barium perchlorate, with ammonium molybdate. It is preferred that the zinc and barium treating agents be used with a carrier to insure intimate contact and simplify handling. Such carriers as silica, bauxite, titania, zirconia, chromia, kieselguhr, bentonite, activated carbon, clays, pumice, and alumina may be used. The various well known co-precipitation, separate precipitation, impregnation, and simple mixing processes may be used to prepare the zinc or barium compound and inert carrier for use in the process. In general between about 5 to 10% by weight of zinc or barium is the desired amount to be incorporated with the carrier. Calculated as zinc molybdate or barium molybdate the amount will be correspondingly higher.

Upon completion of the treatment with zinc molybdate or barium molybdate, the products may sometimes have a slight acrid odor. The odor may be removed by caustic wash since it is apparently due to a trace of sulfur dioxide. The used treating material may be regenerated by passing an oxygen-containing gas through the bed of material at 1100 to 1300 F. The methods of regeneration described in United States Patents 2,506,552, 2,506,545,'and 2,506,542 as applicable to spent contact masses of this type may be used.

What is claimed is:

1. The method of producing special solvent naphthas of petroleum origin from highly refined hydrocarbon mixtures containing small amounts of total sulfur of not more than about 0.16 weight percent which comprises subjecting said hydrocarbon mixtures to contact with at least one reagent selected from the group consisting of zinc molybdate and barium molybdate at a temperature of about 400 to 500 F. and separating special solvent naphthas therefrom characterized by their ability to pass the distillation-corrosion test.

2. The method in accordance with claim 1 in which about 5 to 10% by weight of said contact reagent supported on alumina is used.

3. The method in accordance with claim 1 in which the temperature of contact is about 450 F.

4. The method in accordance with claim 1 in which the hydrocarbon mixtures to be treated are obtained from crude naphthas containing more than about 0.16 weight percent of total sulfur and said crude naphthas are desulfurized at temperatures between about 700 to 800 F. in the presence of a desulfurizing catalyst prior to treatment with said contact reagent.

References Cited in the file of this patent UNITED STATES PATENTS 2,029,100 Grosse Jan. 28, 1936 2,037,791 Ipatiefi Apr. 21, 1936 2,042,298 Davis May 26, 1936 2,422,372 Smith et a1. June 17, 1947

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2029100 *Oct 5, 1931Jan 28, 1936Universal Oil Prod CoTreatment of hydrocarbon oils
US2037791 *Jun 30, 1933Apr 21, 1936Universal Oil Prod CoTreatment of hydrocarbon oils
US2042298 *Aug 31, 1929May 26, 1936Standard Ig CoProcess for the purification and desulphurization of low boiling distillates
US2422372 *Jul 27, 1942Jun 17, 1947Shell DevPreparation of an alumina supported molybdenum oxide catalyst
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2988500 *Mar 13, 1959Jun 13, 1961Universal Oil Prod CoTreatment of hydrocarbon distillates
US4775462 *Jun 22, 1987Oct 4, 1988Uop Inc.Non-oxidative method of sweetening a sour hydrocarbon fraction
U.S. Classification208/189, 502/183, 502/250, 208/250, 502/253, 502/84
International ClassificationC10G29/00
Cooperative ClassificationC10G29/00, C10G17/095
European ClassificationC10G17/095, C10G29/00