GB2123025A

GB2123025A - Solvent extraction of coal by a heavy oil

Info

Publication number: GB2123025A
Application number: GB08219275A
Authority: GB
Inventors: John George Gatsis
Original assignee: UOP LLC
Current assignee: Honeywell UOP LLC
Priority date: 1982-07-02
Filing date: 1982-07-02
Publication date: 1984-01-25
Also published as: FR2529565A1; DE3225029C2; GB2123025B; FR2529565B1; DE3225029A1

Abstract

Coal is mixed with an asphaltene- containing crude petroleum oil and the mixture is subjected to conversion under a hydrogen pressure with a liquid recycle stream containing finely divided unsupported metal catalyst to liquefy the coal and reduce the asphaltene content of the oil, gas is separated from the reaction effluent which is then deashed with a low molecular weight (ie C2-C7) hydrocarbon solvent to separate a heavy liquid phase (containing asphaltenes, unconverted coal, ash and finely divided unsupported metal catalyst) at least a portion of which is recycled to the conversion stage.

Description

SPECIFICATION Improved method of solvent extraction of coal by a heavy oil This invention relates to a process for the conversion of normally solid carbonaceous materials, such as coal, to liquid products. More particularly, this invention relates to a process for the conversion of coal to a liquid product by solvent extraction of the coal using a heavy hydrocarbonaceous liquid containing heptane-insoluble material and a hydrocarbonaceous recycle stream, and recovery of the mixture of the solvent and liquefied coal as the product of the process.

Resources of solid carbonaceous substances, such as coal, lignite and oil shale, represent a valuable source of raw materials for the production of liquid hydrocarbon products commonly obtained from petroleum. The relative abundance of sources of solid carbonaceous materials, with respect to those of petroleum, makes it economically desirable to use these solids to supplement and replace petroleum as energy sources.

Several processes for converting coal to valuable liquid products are known to the art. Recently, high pressure hydrogenation and solvent extraction techniques have been developed, the latter of which is related to the process of this invention. In the processes of solvent extraction known to the prior art, crushed, finely-divided particulate coal, or other solid carbonaceous material, is placed in contact with a liquid solvent which dissolves a part of the solid, usually in the presence of hydrogen gas. Following the contact, the liquid solvent and the liquefied part of the solid are separated from the remaining solid material by filtration, centrifuging or a similar operation.In the other processes known to the prior art, the previously solid material is separated from the solvent, typically by fractional distillation, and is further processed by conventional hydrocarbon processing techniques, such as coking, cracking and hydrogenation, to convert the solvent extracted material into more useful products.

U.S. Patent 3,705,092 discloses a process for the extraction of coal with heavy hydrocarbonaceous liquid while simultaneously improving the quality of the hydrocarbonaceous liquids. The present invention recognizes the fact that this prior art process is improved by recycling at least a portion of the reaction zone effluent. Another example of the typical prior art in the area of coal hydroconversion is U.S. Patent 4,077,867.

One of the problems encountered in the solvent extraction method of liquefying solid carbonaceous substances is the non-selective nature of the solvation which takes place. The process is intended to extract the most valuable. hydrogen-rich fraction of the solid. But solvents which are effective in extracting this hydrogen-rich fraction also liquefy an undesirable fraction containing asphaltenes. Asphaltenes are undistillable compounds of carbon of high molecular weight, and contain less than about 7% of hydrogen by weight. Asphaltenes are also insoluble in normal heptane. They are present not only in the products from solvent extraction of carbonaceous materials, such as coal, but also in petroleum crude oil and fractions thereof, such as topped or reduced crude oils, heavy cycle stocks, visbreaker liquid effluent and the bottom from atmospheric crude towers.The asphaltenic fractions of all these liquid hydrocarbons are of little intrinsic value and interfere with the processing of the more valuable heavy oil fractions with which they are mixed. Thus, the reduction of the asphaltene content in any processable hydrocarbon liquid is a desirable improvement thereof. Further conversion of asphaltenes to distillable hydrocarbons is possible by recycling at least a portion of the reaction zone effluent.

The present invention aims to provide an efficient process for the conversion of solid carbonaceous materials to valuable liquid products and the simultaneous improvement of the properties of a heavy hydrocarbon liquid. More specifically, the invention aims to provide an efficient method for the solvent extraction of valuable liquids from solid carbonaceous materials and the simultaneous conversion of a part of a heavy hydrocarbon liquid from a less desirable material to a more desirable material. In particular the invention aims to provide a method for the efficient solvent extraction of a valuable fraction of a solid carbonaceous material with a concurrent reduction in the asphaltenes contained in a heavy hydrocarbon liquid.

According to the invention, a process for producing hydrogen-enriched hydrocarbonaceous products from hydrocarbonaceous materials comprises contacting coal, as hereinafter defined, and asphaltene-containing petroleum oil in the presence of hydrogen, and a hereinafter described liquid recycle stream containing finely divided, unsupported metal catalyst said metal being selected from the group consisting of Groups IVB, VB, VIB, VIIB and VIII of the Periodic Table of Elements and mixtures thereof in a reaction zone at a temperature from about 1 2.8 OC (55 OF) to about 51 OOC (9500 F) and a hydrogen pressure from about 3450 kPa gauge (500 psi gauge) to about 68,950 kPa gauge (10,000 psi gauge) to liquefy at least a portion of said coal and to reduce the asphaltene content of said oil; and solvent deashing at least a portion of the reaction zone effluent to provide the aforesaid liquid recycle stream which contains said finely divided, unsupported metal catalyst.

In a preferred embodiment of the process in accordance with the invention, comminuted coal is introduced into a solvent extraction zone where it is admixed with a petroleum crude oil and a liquid recycle stream in the presence of hydrogen gas and a finely divided, unsupported metal catalyst at a temperature and pressure which will produce a liquefaction of a portion of the coal.

The crude oil, used as the solvent in the preferred embodiment, contains sufficient heavy oils such that at least 80% of the crude boils above about 343.30C (6500F) and 50% boils above about 5380C (10000F).

In a general embodiment of the present invention, the admixed heavy hydrocarbonaceous liquid solvent, the coal, the liquid recycle stream and the finely divided, unsupported metal catalyst are subjected to sufficient temperature and pressure, in the presence of hydrogen gas, to liquefy the desired fraction of the solid. The solvent extraction and hydrocarbon conversion process may be conducted in either a batch or a continuous reaction vessel. Solvent extraction and hydrocarbon conversion conditions include a temperature of about 1 2.80C to about 51 00C and a pressure of about 3450 kPa gauge to about 68,950 kPa gauge. Hydrogen gas is present at the above-indicated pressure.

The process of the present invention is generally applicable to hydroconvert coal and a heavy hydrocarbonaceous liquid into more valuable hydrocarbonaceous products. The term coal is used herein to designate a normally solid carbonaceous material including all ranks of coal, such as lignite, anthracite, bituminous coal, semi-bituminous coal and mixtures thereof.

The heavy hydrocarbonaceous liquid solvent utilized in the solvent extraction may be any heavy hydrocarbon substance which is liquid at the solvent extraction conditions, contains asphaltenes that are insoluble in normal heptane, and 80% of which boils above about 343.30C and 50% of which boils above about 538"C. The liquid hydrocarbonaceous solvent and coal may be admixed in any weight ratio but a weight ratio from about 1 part solvent to 1 part coal up to about 5 parts solvent to 1 part coal is preferred.

In a preferred embodiment of the present invention, the coal is a bituminous coal having a high content of volatile material. Typically, a high content of volatile material would be about 20% or higher volatiles in the moisture- and ash-free coal. The coal is subjected to extraction and conversion conditions in a finely-divided state. Said finely-divided state is well exemplified by coal particles which pass through about a 200 mesh or finer Tyler sieve.

The liquid hydrocarbonaceous solvent utilized in the preferred embodiment of the present invention is a heavy whole crude oil. Typical of the preferred solvent is a Cold Lake crude oil having an API gravity of about 10 and containing a fraction of materials insoluble in normal heptane of about 8%.

The crude oil, used as the solvent in the preferred embodiment, contains sufficient heavy oils such that at least 80% of the crude boils above 343.30C and 50% boils above 5380C.

In a general embodiment of the present invention, the admixed solvent, the coal and the liquid recycle stream are subjected to sufficient temperature and pressure, in the presence of hydrogen gas, to liquefy the desired fraction of the coal. The solvent extraction process may be conducted in either a batch or a continuous reaction vessel. Solvent extraction conditions include a temperature of about 1 2.80C to about 51 00C and a pressure of about 3450 kPa gauge to about 68,950 kPa gauge.

Hydrogen gas is present at the above-indicated pressure.

Preferably, the admixed solvent, the coal and the liquid recycle stream are processed in a continuous reaction vessel at a flow rate which results in a liquid hourly space velocity of about 0.5 to about 10, where the liquid hourly space velocity is defined as the volumetric flow of the feed per hour divided by the volume of the reactor. The hydrogen gas is recycled to the process from the reactor effluent at a rate of about 888.8 to about 3555 std m3/m3 (i.e. about 5000 to about 20,000 standard cubic feet per barrel) of combined solvent, coal and liquid recycle stream, and hydrogen gas is added to the reaction at a rate sufficient to maintain the above stated range of pressures.

After the reactants have been exposed to the solvent extraction conditions for a length of time sufficient for the desired fraction of the solid to have been liquefied, the reaction zone contents are withdrawn. The gas is separated from the reaction zone effluent. The slurry is solvent deashed under selected process conditions to effect a separation yielding a high grade synthetic crude and a heavy liquid phase. The heavy liquid phase contains high boiling, high molecular weight material, unconverted coal, catalyst and essentially all the mineral matter. A portion of the heavy liquid phase is recycled to the inlet of the reaction zone.

In the preferred embodiment of the present invention, the above-described, finely divided, solid bituminous coal is admixed with the above described heavy petroleum crude oil solvent at a weight ratio of two parts crude oil to one part solid coal. A portion of the subsequently derived liquid stream is recycled to the inlet of the extraction zone at a weight ratio of one part extraction zone effluent to one part solid coal. This mixture of coal, crude oil and liquid recycle stream forms the feed to the reaction or extraction zone, wherein the solvent extraction of this preferred embodiment is maintained. The solvent extraction conditions of the preferred embodiment include a temperature of about 4540C (8500 F) and a hydrogen gas pressure of about 20,680 kPa gauge (3000 psi gauge). The feed to the reaction zone is continuously passed through the reaction zone at a rate sufficient to maintain a liquid hourly space velocity of about 0.5 based on the volume of the fresh feed. Hydrogen gas is recycled to the reaction zone from the reaction zone effluent at a rate of about 2666 std m3/m3 (15,000 standard cubic feet per barrel) of the feed to the reaction zone. The solvent extraction conditions should be maintained so as to produce a conversion of the solid coal to a liquid extract of about 70% by weight of the moisture-andash-free coal.

When the feed to the reaction zone has been subjected to said solvent extraction conditions, it is collected as the effluent from the reaction zone. During the period that the feed was subjected to the solvent extraction conditions, about 70% of the solid coal will have been liquefied to form valuable hydrocarbon products and a part of the crude oil solvent, which was insoluble in normal heptane, will have been converted into a material which is soluble in normal heptane.

The reaction zone effluent after removal of the normally gaseous components is separated by solvent separation to effect separation of the solids from the liquid product. A portion of the solid containing liquid stream is recycled to join the fresh feed to the reaction zone inlet.

The hydrocarbons recovered from the process of the present invention constitute a synthetic crude oil which can be processed in the same manner as any common petroleum crude oil. Both the component derived from the solid and the component derived from the solvent are improved from the process of this invention in that the content of asphaltenes is reduced in both. This reduction in asphaltenes in the synthetic crude oil, particularly with respect to the component derived from the solid, renders the resulting hydrocarbon more readily processable than is the hydrocarbon obtained in the solvent extraction processes known to the prior art.

A suitable liquid recycle stream may be prepared from the whole or a fraction of the extraction zone effluent. A preferred liquid recycle stream is prepared by first removing the normally gaseous components from the extraction zone effluent and then removing the desirable hydrocarbonaceous product with a relatively low molecular weight hydrocarbon solvent in a solvent separation procedure while leaving a component which is well suited for the desired liquid recycle stream and which contains essentially all of the ash, unconverted coal, asphaltenes, relatively high molecular weight hydrocarbons and a finely divided, unsupported metal catalyst.

The solvent separation procedure hereinbefore mentioned is similar to solvent deasphalting processes which are known and described in the prior art. Examples of suitable hydrocarbon-selective solvents are light hydrocarbons including ethane, propane, butane, isobutane, pentane, isopentane, neopentane, hexane, isoheptane, heptane and mono-olefinic counterparts thereof. The prior art has also taught that aromatic hydrocarbons may be added to enhance the solvent.

The finely divided, unsupported metal catalyst is selected from the group consisting of Groups IVB, VB, VIB, VIIB and VIII and mixtures thereof of the Periodic Table of Elements. The finely divided unsupported metal catalyst may be prepared in any convenient method.

The catalyst or catalyst precursor may be an oil soluble metal compound, a finely divided metal or oil insoluble metal compound which is merely suspended in the hydrocarbon oil.

The finely divided, unsupported metal catalyst is generally present in an amount from about 10 WPPM to about 4 weight percent caiculated as the elemental metal, based on the weight of coal in the mixture.

Suitable metal compounds convertible to active catalyst under process conditions include inorganic metal compounds such as oxides, hydrated oxides, sulfides, thiosalts, heteropoly acids, isopolyacids, halides, oxyhalides; metal salts of organic acids, metal salts of organic amines; inorganic and organic metal complexes; organometallic compounds.

Various methods can be used to form the finely divided catalyst but a preferred method of forming the finely divided catalyst from the metal compound is to heat the mixture of metal compound, coal and petroleum oil to a temperature ranging from about 31 5.60C (6000F) to about 426.7 OC (8000 F) and at a pressure ranging from about 3447 to about 34470 kPa gauge (500 to 5000 psi gauge) in the presence of a hydrogen-containing gas. Preferably, the hydrogen-containing gas also comprises hydrogen sulfide. The hydrogen sulfide may comprise from about 1 to about 9G mole percent and preferably from about 1 to 30 mole percent of the hydrogen containing gas mixture.

The conversion of the metal compound into a finely divided metal catalyst according to the above-described method may be performed in a separate catalyst preparation step or process, or, in situ, in the hydroconversion or reaction zone.

The following Example is given to illustrate the process of the present invention and the effectiveness thereof for producing hydrogen-enriched hydrocarbonaceous products from coal and asphaltene-containing petroleum oil. It is not intended that the present invention be unduly limited by the example presented.

Example A 100 g sample of finely divided Illinois No. 6 coal having the following analysis (in percent by weight): Carbon 70.05 Hydrogen 5.88 Oxygen 9.01 Sulfur 2.68 Nitrogen 1.20 Ash 9.02 Moisture (water) 2.15 was charged to a rocker autoclave with a capacity of 1 800 cm3 together with 22.1 g of molybdenum hexacarbonyl and 200 g of Boscan topped crude oil having the following characteristics: 45 Gravity, OKAPI at 15.5 C 5.5 Distillation, IBP,OF 693 5% 769 10% 804 30% 977 EP 977 % Over (volume) 30.5 Carbon, wt% 82.8 Hydrogen, wt% 10.6 Nitrogen, wt% 0.8 Sulfur, wt% 5.6 Vanadium, ppm 1500 Nickel, ppm 130 Heptane insolubles, wt% 19.04 The autoclave was then pressured with a 10/90 hydrogen sulfide-hydrogen mixture to about 7583 kPa gauge and then pressured with pure hydrogen to about 10,341 kPa gauge. The charged autoclave was then heated to a temperature of about 390 C and maintained at a pressure of about 1 7,235 kPa gauge for one hour. The cooled contents of the autoclave were recovered with a toluene rinse.After the toluene was flashed, the product was solvent separated with isopentane at four volumes of isopentane for each volume of autoclave product. The isopentane soluble fraction was recovered and the isopentane was removed by flashing. The solvent free isopentane soluble product weighed 185.8 g.

The isopentane insoluble fraction which weighed 56.3 g and contained the finely divided unsupported metal catalyst was recycled with 100 g of Illinois No. 6 coal and 200.7 g of Boscan topped crude oil to the autoclave. The above-described heating and pressuring of the autoclave was repeated in an identical fashion. Here again the cooled contents of the autoclave were recovered with a toluene rinse.

After the toluene was flashed, the product was solvent separated with isopentane at four volumes of isopentane for each volume of autoclave product. The isopentane soluble fraction was recovered and the isopentane was removed by flashing. The solvent free isopentane soluble product weighed 98.4 g.

The isopentane insoluble fraction which weighed 118.4 g and contained the finely divided unsupported metal catalyst was recycled with 100 g of Illinois No. 6 coal and 198.1 g of Boscan topped crude oil to the autoclave. The corresponding heating, pressuring and subsequent separating as described above was aaain reDeated in an identical fashion. The solvent free isopentane soluble product weighed 1 89.7 g and the isopentane insoluble fraction weighed 178.7 g. The most recent isopentane insoluble fraction weighing 178.7 g was charged to the autoclave with 100 g of Illinois No. 6 coal and 188.1 g of Boscan topped crude oil. The above-described autoclave process was again performed to yield an isopentane soluble product weighing 164.1 g and an isopentane insoluble fraction weighing 186.7 g.

The resulting isopentane insoluble fraction was solvent extracted with toluene to yield 130.7 g of toluene soluble material which is useful for heavy fuel oil and 51.1 g of toluene insoluble material which contained unconverted coal, mineral matter and catalyst.

The four autoclave runs are summarized in Table I and the toluene extraction of the isopentane insolubles is summarized in Table II.

Table I Summary of batch recycle autoclave runs Run no. 1 2 3 4 Charge Coal, g 100 100 100 100 Topped Boscan oil, g 200 200.7 198.1 188.1 Mo(CO)6,g 22.1 - - - Recycle, g - 56.3 117.3 177.9 Product recovery Toluenefree,g 261.1 221.5 381.1 422.0 Isopentane soluble, g 185.8 98.4 189.7 164.1 Carbon, wt% 86.22 84.03 Hydrogen, wt% 11.44 10.78 Oxygen, wt% 0.17 0.10 Sulfur, wt% 2.77 3.17 Nitrogen, wt% 0.43 0.56 Nickel, ppm 2.7 1.8 Vanadium, ppm < 1 18 Heptane insoluble, wt% < 0.01 0.3 Isopentane insoluble, g 56.3 11 8.4 178.7 186.7 Table II Toluene extraction of the isopentane insolubles Charge, g 186.7 Toluene soluble Toluene in soluble Recovered weight, g 130.7 51.1 Carbon, wt% 84.74 31.60 Hydrogen, wt% 7.66 3.04 Oxygen, wt% 2.73 Sulfur, wt% 2.36 14.1 Nitrogen, wt% 1.43 Molybdenum, wt% 6.70 Vanadium, wt% 1.73 Nickel, wt% 0.15 Iron, wt% 6.8 From the foregoing description and Example, it is apparent that the process of the present invention provides a superior method for producing hydrogen-enriched hydrocarbonaceous products from coal and asphaltene-containing petroleum oil.

Claims

1. A process for the production of hydrogen-enriched hydrocarbonaceous products from hydrocarbonaceous materials which comprises: (a) commingiing coal and a crude petroleum oil containing asphaltenes and heavy oil in an amount such that at least 80% of the crude boils above 343.30C;; (b) subjecting the resultant mixture to conversion together with a hereinafter described liquid recycle stream containing finely divided, unsupported metal catalyst in which the metal is selected from the group consisting of the elements from Groups IV, VB, VIB, VIIB and VIII of the Periodic Table of Elements and mixtures thereof in a reaction zone at a temperature from about 1 2.80C to about 51 00C and a hydrogen pressure from about 3450 kPa gauge to about 68,950 kPa gauge to liquefy at least a portion of said coal and to reduce the asphaltene content of said oil; (c) separating gas from the resultant reaction zone effluent;; (d) then solvent deashing at least a portion of the reaction zone effluent with a relatively low molecular weight hydrocarbon solvent to separate therefrom a heavy liquid phase containing substantially all of the ash, unconverted coal, asphaltenes, relatively high molecular weight hydrocarbons and finely divided, unsupported metal catalyst; and (e) supplying at least a portion of said heavy liquid phase to the reaction for use as said liquid recycle stream in the aforesaid step (b).

2. A process according to claim 1, wherein said asphaltene-containing petroleum oil has a 50% boiling point greater than about 5380C.

3. A process according to claim 1 or 2, wherein said finely divided unsupported metal catalyst comprises molybdenum.

4. A process according to claim 1 or 2, wherein said finely divided unsupported metal catalyst comprises vanadium.

5. A process according to any of the preceding claims, wherein the weight ratio of asphaltenecontaining petroleum oil to coal is from about 1:1 to about 5:1.

6. A process according to any of the preceding claims, wherein the liquid flow rate in said reaction zone results in a liquid hourly space velocity of about 0.5 to about 10.

7. A process according to any of the preceding claims, wherein the hydrogen circulation rate in said reaction zone is from about 888.8 to about 3555 std m3/m3 based on the reaction zone charge.

8. Hydrogen-enriched hydrocarbonaceous products when produced by the process claimed in any of the preceding claims.

9. The hydrogen-enriched hydrocarbonaceous products produced by the process described in the foregoing Example.