US2568841A

US2568841A - Method of synthesizing gasoline hydrocarbons

Info

Publication number: US2568841A
Application number: US725836A
Authority: US
Inventors: George B Arnold; Howard V Hess
Original assignee: Texaco Inc
Current assignee: Texaco Inc
Priority date: 1947-02-01
Filing date: 1947-02-01
Publication date: 1951-09-25
Anticipated expiration: 1968-09-25

Description

Sept 25, 1951 G. B. ARNOLD ET AL METHOD OF SYNTHESIZING GASOLINE HYDROCARBONS Filed Feb. l, 1947 massacres;

METHOD F SYNTHESIZING GASOLINE HYDROC of Delaware ABBONS Geom arnold, Gienhm, N. Y., 'ma norma V. Hess, Charleston, W. Va., assignors to The Texas Company, New York, N. Y., a corporation Application February l, 1947. Serial No. '125,838

11 Claims.l (Cl. ZBO-450) l This invention relatos to a method of synthesisv gasconversion and more particularly' to a meth od oi' catalytically converting synthesis gas so that a greater portion of the product comprises liquid hydrocarbons in the gasoline boiling range.

In accordance with the invention, synthesis gas comprising carbon monoxide and hydrogen is catalytlcally converted in a reaction zone to a product mixture comprising hydrocarbons, oxygen-containing compounds and water, which mixture is separated into a gas phase, a liquid hydrocarbon phase and a water phase, which latter two phases contain dissolved therein substantial quantities of oxygen-containing compounds. The gas phase containing normally gaseous productsv of conversion and unreacted carbon monoxide and hydrogen is recycled at least in part to said reaction zone. 'I'he aqueous phase containing dissolved therein mainly low molecular weight oxygen-containing compounds is sub- Jected at elevated temperature and pressure t0 extraction with a hydrocarbon solvent so as to form a hydrocarbon-rich extract phase containing most of the non-acidic oxygen-containing compounds and a water-rich phase containing low molecular weight organic acids. The hydrocarbon-rich extract phase is combined with the liquid hydrocarbon phase which is initially sepreaction zone so as to eilect conversion of the taining compoundsfrom the hydrocarbon solution. As a result of the extraction, there are formed a hydrocarbon raiiinate which is substanv tially free from oxygen-containing compounds and a solvent-rich extract phase containing extracted oxygen-containing compounds. The hydrocarbon raillnate is then subjected to such further treatment as will improve its quality in its intended use. CXygen-containing compounds are separated from the extract phase.

2 Even when'the catalytic conversion of 'carbon monoxide and hydrogen 'is directed mainly towards the production of liquid hydrocarbons in the gasoline range, the conversion is accompanied by the formation of considerable quantities of oxygen-containing organic compounds. 'I'hese oxygen-containing organic compounds comprise alcohols. aldehydes, ketones, esters and organic acids with the alcohols forming by far the greatest portion of the oxygen-containing organic byproducts. In a typical synthesis operation directed towards the production oi gasoline hydrocarbons, the oxygen-containing organic compounds produced may amount to as much as 20 weight per cent of the total organic compounds produced. The lower boiling oxygen-containing organic compounds such as ethyl, propyl and butyl alcohols, together with low boiling aldehydes such as ethanal, propanal and butanal, ordinarily comprise a large proportion of the total oxygen-containing compounds produced. This invention provides a method oi converting such low boiling oxygen-containing compounds, which are not as valuable economically as the higher boiling oxygen-containing compounds, into liquid hydrocarbons boiling in the gasoline range or higher boiling oxygen-containing compounds.

When the product of synthesis gas conversion is separated into a gas phase, a liquid hydrocarbons phase and an aqueous phase at atmospheric conditions, most of the low boiling oxygen-containing compounds, that is, compounds containing 4 or less carbon atoms, are present 'in the aqueous phase. This invention provides a method of transferring these low boiling oxygen-containing compounds to the hydrocarbon phase whence they may be recycled, together with a low boiling -hydrocarbon fraction, to the synthesis unit.

The recycling of a part of the' hydrocarbon fraction ofthe products which boils below about 200 to 245 F. and which contains substantially all of the non-acidic low boiling oxygen-contain# ing compounds produced in the conversion, has a two-told benecial effect in increasing the yield of gasoline hydrocarbons produced by the synthesis reaction: iirst, the low boiling oxygen-containing compounds which comprise the alcohols produced in the conversion up to and including butyl alcohol, aldehydes up to and including pentanal and ketones upto and including methyl propyl ketone are converted into gasoline hydrocarbons; further, low boiling olens such as propylenes, butylenes and amylenes which are present both in the recycle gas phase separated from the products and in the recycle portion of accessi 4 I a temperature at this point but this 3 thelowboilinghydrocarbonfractbmareeon verted into compounds or higher mo weightinthesynthesisscnesothatahigher timate yield of product boiling in the gasoline range is obtained. .A further advantage resides in the fact that the presenceoi liquid hydrocarbons boiling up to about 245 F. absorbs a conslderable portion of the liberated exothermic heat of reaction, thereby minimizing the problem of temperature control in the catalytic conversion of carbon monoxide and hydrogen. The method of the invention has an additional advantage when a fluid dense phase type of catalytic oonversion is employed; the presence of a substantial quantity of recycle hydrocarbons can be used to oil'set at least to some extent the volume decrease accompanying the conversion of carbon monoxide and hydrogen into liquid hydrocarbons and the like.

In' continuous operation, the product of synthesis gas conversion is initially separated into a gas phase, an aqueous phase and a liquid hydrocarbon phase at elevated temperature and presnot only places an added burden on the extraction of the aqueous phase, but also necessitates the reheating oi the aqueous phase prior to its extraction with a liquid hydrocarbon fraction.

The total product is introduced through a pipe I into a separator I wherein the aqueous phase is separated from both the normally liquid hydrocarbon phase and the normally gaseous products sure. The separation of the product into these phases at elevated temperature and pressure reduces the heat requirements of the process since it is not necessary to reheat the aqueous phase prior to extraction with a hydrocarbon solvent. Moreover, initial separation of the product at a temperature of about 200 to 300 F. and at a pres- 4sure o1' about 150 to 300 pounds per square inch displaces a portion of the lower, boiling oxygencontaining compounds from the aqueous phase to the hydrocarbon phase, thus minimizing the burden in the solvent extraction of the aqueous phase so that smaller solvent dosages and a smaller extraction tower may be employed.

In order th'at the invention may be more adequately described, reference will now be made to the accompanying figure in which a preferred modification of the process of the invention is Presented in detail.

Carbon monoxide and hydrogen in a molecular ratio which is usually about 2 mols of hydrogen t0 1 mol of carbon monoxide are obtained from a source not shown and introduced into a synthesis unit 2 through a pipe I. In the synthesis unit 2, the reactants may be subjected to contact with a synthesis catalyst in the form of a iluidized mass of solid particles or powder. A catalyst having iron as its main constituent is advantageously used to effect this conversion although other synthesis catalysts containing cobalt or nickel may be employed. The synthesis catalyst may also comprise alkali metal compounds and the oxides of metals such as thorium, magnesium, aluminum, uranium and vanadium.

A catalyst having a composition of about 93- 98 per cent iron, about 2-7 per cent alumina and about 0.1 to 3 per cent alkali expressed as potassium oxide has been found to be particularly effective for the conversion. The synthesis reaction with such a catalyst is usually carried out at a temperature of about 500 to 700 F. and under a pressure of about 150 to 300 pounds per squareinch in order to yield liquid hydrocarbons boiling in the gasoline range as the primary product of conversion.

An eiliuent stream comprising the products of synthesis reaction and unreacted carbon monoxide and hydrogen leaves the synthesis unit 2 through a pipe 3 and is cooled to a temperature of about 175 to 300 F. and preferably to about 200 to 225 F. in an exchanger 4. As has been indicated previously, the eluent may be cooled to about of conversion. The separator l is maintained, for example, at a temperature o! about 200 F. and at a pressure of about to 300 pounds per square inch. The aqueous phase is withdrawn from the separator l through a conduit 1. Both the gas phase and the liquid hydrocarbon phase are removed from the upper portion oi' the separator l through a pipe l and are cooled to approximately atmospheric conditions in the exchanger Il prior to introduction into a secondary separator I I which is maintained at about atmospheric conditions of temperature and pressure. In the separator I'I, the liquid hydrocarbon phase is separated from the gas phase. The liquid hydrocarbon phase is withdrawn from the separator Ii through a pipe i2 and its further treatment will be described more in detail later. The gas phase. containing unreacted synthesis gas and normally gaseous products oi' conversion, such as ethane, methane, carbon dioxide, etc., leave the separator Il through a pipe il. Some additional aqueous phase separates in a secondary atmospheric separator li and is withdrawn therefrom through a pipe I3.

The gas phase withdrawn from the separator Ii is recycled at least in part to the synthesis unit 2. The portion of the gas phase which is to be recycled proceeds along the pipe i4 and combines with the fresh feed to the synthesis unit. 2 in the pipe I. There may be employed recycle ratios of 0.25 to 4 wherein recycle ratio is expressed as moles of recycle gas per moles of fresh feed. A vent i5 serves as a means of withdrawing the non-recycled portion of the gas phase which portion may be treated so as to recover valuable constituents such as butanes therefrom.

The additional water phase which separates in the separator il flows through the pipe I2 into the conduit 'l wherein it combines with the aqueous phase initially separated from the products of conversion. Combined aqueous phases are then introduced into a primary extraction tower 2l which is maintained at a temperature of about 200 F. and at a pressure of about 200 to 250 pounds per square inch. f

In the extraction tower 20, combined aqueous phases are subjected to countercurrent extraction with a hydrocarbon solvent such as naphtha which is introduced therein through a pipe 22. Under the specified conditions of temperature and pressure prevailing within the extraction tower, the bulk of the non-acidic oxygen-containing organic compounds are substantially extracted from the water phase. As a result ofthe countercurrent extraction in the tower 20, there are formed a hydrocarbon-rich extract phase containing non-acidic oxygen-containing organic compounds and a water-rich phase containing low molecular weight organic acids.

The water-rich phase containing low molecular weight organic acids is withdrawn from the extraction tower 20 through a pipe 23 and the residual low boiling non-acidic oxygen-containing compounds which are predominantly ethyl alcohol may be removed as aqueous aseotropes byilashinginaiiashtowergj. Theaqueous 8 aaectropes comprising mainly ethyl alcohol-- water azeotrope which has a composition of about 95.5% alcohol and 4.5% water is recycled through a pipe 2l to the synthesis unit for conversion to hydrocarbons in the gasoline range.

Thereafter, the water-rich phase can be introducedthrough a pipe 2l into a fractionating tower, not shown. in which the water may be distilled from the organic acids by azeotropic distillation with a hydrocarbon fraction. The

organic acids may then be separated into individual. components byfractionation.

The hydrocarbon-rich extract phase containing extracted non-acidic oxygen-containing organic compounds leaves the extraction tower 2l through a pipe 21. 'I'his extract phase proceeds along the pipe 21 and combines in the pipe I2 with the hydrocarbon phase initially separated from the products of conversion. The combined mixture containing substantially all of the nonacidic oxygen-containing compounds produced in the conversion which includes aldehydes, ketones, alcohols and esters is introduced into a fractionating tower 28.

In the fractionating tower 28, the mixture of hydrocarbons and oxygen-containing compounds is divided into two fractions: a low boiling fraction distilling below a temperature which lies in the range of about 200 to 245 F. is taken ori overhead through a pipe 29; the residual fraction, containing all the products of conversion distilling above the chosen temperature of division, is withdrawn from the lower portion of the fractionating tower 28 through .a pipe 30. If 245 F. is chosen as the temperature at which decaan Y f 8 version is diverted pipe 34 ,and combines with the high boiling residual hydrocarbon and oxygen-.containing products which were withc'irawnV from the fractionating tower 28S through a pipe. and thereafter cooled in the exchanger .35. 'I'he combined hydrocarbon phases are introduced through a pipe 38 into a secondary extraction tower 31 which is advantageously packed with contact material.

Therein the combined hydrocarbon` phases con.

cible with hydrocarbons under operating. conditions which are usually atmospheric. A solvent the mixture is split into fractions, the overhead fraction will contain hydrocarbons containing up to and including about 8 carbon atoms per molecule, alcohols up tol and including butyl alcohol, aldehydes up to andincluding pentanal and ketones up to and including methyl propyl ketone.

The low boiling fraction which leaves the fractionating tower 28 through the pipe 29 is divided into two portions. The major portion is passed along the pipe 3| through which it is recycled to the synthesis unit 2. This major portion of the low boiling fraction of the productsof conversion flows through the pipe 8| into the pipe I4 through which gaseous products of conversion are recycled to the synthesis unit 2. In

the method of the invention, therefore, the total feedto the synthesis unit 2 comprises fresh synthesis gas, normally gaseous products of conversion comprising carbon dioxide, methane, ethane, etc., and the major portion of the hydrocarbons and oxygen-containing hydrocarbons distiuing below about 20o to 245 F.

As has been indicated, the paramount beneiicial eilect accompanying the recycle of hydrocarbons and oxygen-containing products distilling below 200 to 245 F. is realized in the improved yield of liquid hydrocarbons distilling within the gasoline range thereby obtained. 'I'his invention provides a simple expedient of converting such oxygen-containing compounds to high-grade fuel. The yield oi' gasoline hydrocarbons may be increased as much as 10 per cent when low boiling hydrocarbons and oxygencontaining compounds are recycled to the synthesis unit as described in this invention; such an improvement is signicant in a commercial unit making about 5,000 barrels per day of gasoline hydrocarbons.

The minor portion of the low boiling hydrocarbon and oxygen-containing products of con- 'such as ethylene glycol is introduced into the extraction tower 31 through a pipe 38 and therein is contacted countercurrently with the hydrocarbon solution of oxygen-containing compounds flowing upwardly therethrough. As a result of the secondary extraction, there are formed a hydrocarbon-rich ramnate winch is substantially Vfree from alcohols, aldehydes and ketones and a solvent-rich extract phase containing most of the unrecycled alcohols, aldehydes and ketones produced in the process. together with some of the ester products.

Ethylene glycol has proven to be an excellent solvent for effecting the extraction of aldehydes, ketones and alcohols from the hydrocarbon solution. However, it is contemplated that other hydrocarbon-immiscible solvents such as polyolen glycols, aldehydes such as furfural, ketones such as acetone and nitrohydrocarbons such as nitromethane may be employed for the solvent extraction of alcohols. aldehydes and ketones from the hydrocarbon solution. In further description of the invention, it will be assumed that ethylene glycol has been used to effect the extraction of the oxygen-containing compounds from the hydrocarbon phase.

The hydrocarbon-rich raiilnate is withdrawn from the upper portion of the extraction tower 31 through a pipe 40 and is thereafter waterwashed in a wash tower 4I for the removal of any residual glycols dissolved therein. To this end, water is introduced into the wash tower 4| through a pipe 4'2 in the ratio of about one volume of water to 10 volumes of hydrocarbon. The washed hydrocarbons are withdrawn from the upper portion of the wash tower 4I through a pipe 43. A portion of this hydrocarbon fraction,

which is substantially free from oxygen-containing compounds. can be used to effect the extraction of non-acidic oxygen-containing compounds from the water phase in the primary extraction tower 20. Accordingly a portion of the washed hydrocarbon solution is diverted from the pipe 43- through a pipe 44 which latter pipe communicates with pump 45 and exchanger 46 wherein the hydrocarbon fraction is raised to a pressure of about 200 pounds per square inch and a temperature of about 200 F. The pipe 44 communicates with the pipe 22 and from there flows into the primary extraction tower 20.

The remainder of the washed hydrocarbons obtained from the wash tower 4i pass through a pipe 4.1 to a fractio ating tower 48 wherein it is separated into a gaso e fraction and a diesel fraction. The gasoline fr ction is taken oil overhead from the fractiona g tower 48 through a pipe 48 and thereafter be subjected to from the pipe 29 through a.

l treatment 'with a material such as bauxite for the improvement ofits octane rating. The diesel fraction is obtained from the iractionating tower 4I through a pipe lo and may undergo treatment such as contacting with silica gel which will remove any residual high molecular weight oxygen-containing compounds still present ltherein. The diesel fraction may also be eatalytieally or thermally cracked to yield more gasoline hydroearbons. The high boiling residuum is withdrawn from the i'ractionatingtower 48 through 4 a pipe Il.

Solvent-rich extract phase containing dissolved therein mainly alcohols, aldehydes and ketones is withdrawn from the lower section of the secondary extraction tower 31 through a. pipe Il and is introduced into a fractionating tower it. Therein alcohols up to and including C7 alcohols, aldehydes and ketonesdistilling below the boiling point of ethylene glycol, namely about 388 F., are separated by fractional distillation from the solvent and from the higher boiling oxygencontaining compounds. It should be noted that the process of the invention produces only a small quantity of such lower boiling alcohols, aldehydes and ketones because the maior portion of the oxygen-containing products distilling below 245 F. are converted into hydrocarbons in the gasoline range by recycling them to the synthesis unit. The low boiling oxygen-containing compounds are removed as a distillate from the fractionatlng tower lthrough a pipe 51.

The glycol solution of high boiling oxygen-containing compounds is removed from the bottom portion of the iractionating tower 56 through a pipe 58 and introduced into a distilling tower 59. The water from the wash tower Il which contains ethylene glycol and oxygen-containing compounds which were washed from the hydrocarbon railinate is also introduced into the distilling tower 59 through pipes 60 and 5l. In the distilling tower S, high boiling alcohols, aldehydes and ketones are steam distilled from the ethylene glycol solvent as water azeotropes which leave the tower 59 through a, pipe 62 and flow into a settler 65 after condensation in an exchanger 63.

Glycol from whichhigher boiling oxygen-containing compounds have been steamdistilled is withdrawn from the distilling tower 5l through a pipe Il and is therethrough recycled to the secondary extraction tower 31. The pipe ll communicates with the pipe 38 which serves as the entry pipe for the hydrocarbon-immiscible solvent.

Since the high boiling oxygen-containing compounds are only sparingly soluble in water, they are readily separated from the condensate consisting oi water and high boiling oxygen-containing compounds. Water is withdrawn from the lower portion of the settler Il through a pipe li. The higher boiling oxygen-containing compounds are withdrawn from the settler through a pipe 68. The combined alcohols. aldehydes and ketones may be subjected to mild catalytic hydrogenation in order to convert aldehydes and ketones into alcohols. 'Since the oxygen-containing compounds are mainly in the form ofaleohois as a result of this treatment, they are readily separated into individual compounds by close fractionation. Individual alcohols may be reoxidized to aldehydes and ketones if such compounds are desired.

In the description of the invention, the proda liquid hydrocarbon phase and an aqueous phase at elevated temperature and pressure which aqueous phase is then extracted with a hydrocarbon solvent at elevated temperature and prsure. It is contemplated that the initial separation of the. products of conversion into an aqueous phase and a hydrocarbon phase at elevated temperature and pressure may eil'ect such a displacement of low boiling oxygen-containing compounds from the aqueous phase to the liquid hydrocarbon phase that the subsequent step of separately extracting the aqueous phase with a hydrocarbon solvent may not be necessary. Consequently, the synthesis product may be separated at elevated temperature and pressure into an aqueous phase and a liquid hydrocarbon phase which is directly introduced into a fractionating tower for separation into a high-boiling fraction and a low boiling fraction, a portion of which is recycled to the synthesis unit. The extraction of the aqueous phase with a hydrocarbon solvent is eliminated in this instance.

It is contemplated that oxygen-containing compounds may be recycled to the synthesis reaction in the form of their aqueous azeotropes. In the detailed description of the invention, there i.: shown the recycle of ethyl alcohol to the synthesis unit in the form of its aqueous azeotrope. There is included within the scope of the invention the introduction of other low-boiling oxygencontaining compounds in the form of the aqueous azeotropes, in which form they are readily separated from the aqueous phase by distillation.

It is further contemplated that low-boiling oxygen-containing compounds can be recycled to the synthesis unit without employing a hydrocarbon carrier. This can be accomplished by extracting the oxygen-containing compounds from the hydrocarbon phase of the synthesis product. then separating the oxygen-containing compounds from the extract phase and recycling a low boiling fraction of the oxygen-containing compounds to the synthesis unit.

Obviously many modications and variations of the invention, as hereinbefore set forth, may be made without departing from the spirit and scope thereof and. therefore. only such limitations should be imposed as are indicated in the appended claims.

We claim:

l. In the catalytic conversion of carbon monoxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at a temperature of about 500 to 700 F., to form a product mixture comprising mainly hydrocarbons, water and oxygen-containing organic compounds comprising alcohols, aldehydes, ketones, esters and acids, separating said product mixture into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide and hydrogen, a liquid hydrocarbon phase and an aqueous phase, separating from said hydrocarbon phase and said aqueous phase said oxygen-containing organic compounds distilling below about 245 F. and recycling at least a portion of said oxygen-containing compounds to said conversion zone so as to increase the yield of liquid hydrocarbons in the gasoline range.

2. In the catalytic conversion ot carbon monoxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method uct of synthesis gas conversion is separated into Il which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at-a temperaturey o! about 500 to 700 F. to form a product mixture comprising mainly hydrocarbons. w'ater and oxygen-fountaining organic compounds comprising alcohols, aldehydes, ketones, esters and acids, separating said product mixture into a gas phase comprising normally gaseous products oi'conversion and unref acted carbon monoxide and hydrogen. a liquid oxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at a temperature of about 500 to '700 F. to form a product mixture comprising mainly hydrocarbons, water and oxygen-containing organic compounds comprising alcohols, aldehydes, ketones, esters and acids, separating said productI mixture into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide and hydrogen, a liquid hydrocarbon phase and an aqueous phase, recycling at least a portion of said gas phase to said conversion zone and recycling at least a portion of said liquid hydrocarbon phase distilling below about 245 F. and containing low boiling oxygen-containing organic compounds to said conversion zone so as to increase the yield of liquid hydrocarbons boiling in the gasoline range.

4. In the catalytic conversion of carbon monoxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method which comprises catalytically' reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at aftemperature of about 500 to '700 F. to form a product comprising mainly hydrocarbons, water and oxygen-containing organic compounds comprising alcohols, aldehydes, ketones, esters and acids, separating said product mixture at elevated temperature between 175 and 300 F. and elevated pressure of about 150 to 300 pounds per square inch into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide and hydrogen, a liquid hydrocarbon phase and an aqueous phase, recycling a major portion of said liquid hydrocarbon phase distilling below about 245 F. and containing low boiling oxygen-containing organic compounds to said conversion zone so as to increase the yield of liquid hydrocarbons in the gasoline range.

5. In the catalytic conversion of carbon monoxide and hydrogen for the production of liquid hydrocarbons inthe gasoline range, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at a temperature of about 500 to 700 F. to form a. roduct mixture comprising mainly hydrocarbons, water and oxygen-containing organic compounds comprising alcohols, aldehydes, ketones, esters and acids, separating said product mixture into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide and hydrogen, a liquid hydrocarbon phase and an aqueous phase, fractionating said liquid hydrocarbon phase into a fraction distilling below about 245 F. and concrease theyield of liquid hydrocarbons in the gasoline 6. In the catalytic conversionV ofcarbon monoxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at a temperature of 500 to 700 F. to form a product mixture comprising mainly hydrocarbons, water and oxygen-containing organic compounds comprising alcohols, aldehydes. ketones, esters and acids, separating said product mixture at elevated temperature and elevated pressure into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide and hydrogen, a liquid hydrocarbon phase and an aqueous phase, recycling at least a portion of said gas phase to said conversion zone, fractionating said liquid hydrocarbon phase at atmospheric pressure into a low boiling fractionvdistilling below about 245 F. and a high boiling fraction distilling above about 245 F. and recycling a major portion of said low boiling `fraction to said conversion zone so as to increase the yield of liquid hydrocarbons in the gasoline range.

7. In the catalytic conversion of carbon monoxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone to form a product mixture 'comprising mainly hy drocarbons, oxygen-containing compounds and water, separating said product mixture into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide and hydrogen, a liquid hydrocarbon phase and an aqueous phase, both of the latter two phases containing substantial quantities of oxygen-containing hydrocarbons, recycling at least a portion of said gas phase to said conversion zone, subjecting said aqueous phase to extraction with a hydrocarbon solvent at elevated temperature and pressure so as to form a hydrocarbon-rich extract phase containing non-acidic oxygen-containing hydrocarbons and a water-rich phase containing organic acids, combining said extract phase with said liquid hydrocarbon phase which was initially separated from said product mixture, fractionating said combined phases at atmospheric pressure into a low boiling fraction distilling below about 245 F. and a high boiling fraction :distilling above about 245 F. and recycling a portion of said low boiling fraction to said conversion zone so as to increase the yield ofliquid hydrocarbons in the gasoline range.

8. In the catalytic conversion of carbon monoxide and hydrogen for the production of liquid hydrocarbons in the gasoline range, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone to form a product mixture comprising mainly hywater, separating said product mixture at ele-- drocarbons, oxygen-containingfcompounds and vated temperature and elevated pressure into a gas phase comprising normally gaseous products of conversion and unreacted carbon monoxide ,and hydrogen, a liquid'hydrocarbon phase and an aqueous phase, both of the two phases containing substantial quantities of oxygen-containing hydrocarbons, recycling atleast a portion of said gas phase to said conversion zone. sub- Jecting said aqueous phase to extraction with a aliphatic hydrocarbon solvent at elevated temperature and pressure so as to form a hydrocarbon-rich extract phase containing non-acidic oxygen-containing hydrocarbons and a waterrich phase containing' organic acids, combining said extract phase with said liquid hydrocarbon phase which was initially separated from said product mixture, fractionating said combined phases into a low boiling fraction distilling below about 245 F. and a high boiling fraction distilling above about 245 F. and recycling a major portion of said low boiling fraction to said conversion zone so as to increase the yield of liquid hydrocarbons in the gasoline range.

9. The method according to claim 8 in which the separation of the product mixture and the extraction of the aqueous phase are effected at substantially equivalent conditions, namely about 20 water and oxygen-containing organic compounds 30 comprising alcohols, aldehydes, ketones, esters and acids, separating said oxygen-containing compounds from said hydrocarbon phase and said water phase, and recycling at least a porl2 tion of said oxygen-containing compounds which are vaporizable under reaction conditions to said conversion zone so as to increase the yield of liquid hydrocarbons. l

11. In the catalytic conversion or carbon monoxide and hydrogen to produce liquid hydrocarbons, the method which comprises catalytically reacting carbon monoxide and hydrogen in a conversion zone in the vapor phase at a temperature of about 500 to 700 F. to form a prod/- uct mixture comprising mainly hydrocarbons. water and oxygen-containing organic compounds comprising alcohols, aldehydes, ketones, esters and acids, separating said oxygen-containing compounds from said hydrocarbon phase and said Water phase and recycling at least one of said oxygen-containing compounds which are vaporizable under reaction conditions in substantial amount to said conversion zone so as to increase the yield of liquid hydrocarbons.

GEORGE B. ARNOLD. HOWARD v. Hass.

REFERENCES CITED The following references are of record in the flle of this patent:

UNITED STATES PATENTS

Claims

1. IN THE CATALYTIC CONVERSION OF CARBON MONOXIDE AND HYDROGEN FOR THE PRODUCTION OF LIQUID HYDROCARBONS IN THE GASOLINE RANGE, THE METHOD WHICH COMPRISES CATALYTICALLY REACTING CARBON MONOXIDE AND HYDROGEN IN A CONVERSION ZONE IN THE VAPOR PHASE AT A TEMPERATURE OF ABOUT 500 TO 700* F., TO FORM A PRODUCT MIXTURE COMPRISING MAINLY HYDROCARBONS, WATER AND OXYGEN-CONTAINING ORGANIC COMPOUNDS COMPRISING ALCOHOLS, ALDEHYDES, KETONES, ESTERS AND ACIDS, SEPARATING SAID PRODUCT MIXTURE INTO A GAS PHASE COMPRISING NORMALLY GASEOUS PRODUCTS OF COVERSION AND UNREACTED CARBON MONOXIDE AND HYDROGEN, A LIQUID HYDROCARBON PHASE AND AN AQUEOUS PHASE, AND SAID RATING FROM SAID HYDROCARBON PHASE AND SAID AQUEOUS PHASE SAID OXYGEN-CONTAINING ORGANIC COMPOUNDS DISTILLING BELOW ABOUT 245* F. AND RECYCLING AT LEAST A PORTION OF SAID OXYGEN-CONTAINING COMPOUNDS TO SAID CONVERSION ZONE SO AS TO INCREASE THE YIELD OF LIQUID HYDROCARBONS IN THE GASOLINE RANGE.