US1940648A - Process for obtaining valuable distillates from carbonaceous materials - Google Patents
Process for obtaining valuable distillates from carbonaceous materials Download PDFInfo
- Publication number
- US1940648A US1940648A US334148A US33414829A US1940648A US 1940648 A US1940648 A US 1940648A US 334148 A US334148 A US 334148A US 33414829 A US33414829 A US 33414829A US 1940648 A US1940648 A US 1940648A
- Authority
- US
- United States
- Prior art keywords
- oil
- drum
- suspension
- carbonaceous materials
- vapor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
- C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
Definitions
- the present invention comprises an improved process for obtaining valuable low boiling oils from carbonaceous materials such as petroleum, tars and the like and also from solid carbona- 5 ceous materials especially those, which like coal, contain solid foreign matter.
- carbonaceous materials such as petroleum, tars and the like
- solid carbona- 5 ceous materials especially those, which like coal, contain solid foreign matter.
- the drawing is a semi-diagrammatic view in sectionalzelevation of an apparatus constructed according to my invention and indicates the fiow of materials.
- reference numeral 1 denotes a pipe coil arranged in a suitablefurnace setting 2 and adapted to heat a stream of hydrocarbon oil or the like to an elevated temperature.
- the coil discharges into a reaction chamber 3 which is constructed to withstand high internal pressure and high temperature,
- the contents of the drum is kept in thorough agitation by means of a stirrer 4 or the like and the temperature of the drum is maintained at the desired level in any suitable manner, for example, by the use of internal electrical heaters. but I prefer to continuously withdraw apart of the oil by pipe 5 and circulate the same by means of a suitable pump 6 back to drum 3 by way of coil 1. Hydrogen or a gas rich in free hydrogen is withdrawn from a suitable source (not shown) by pipe 7, compressed by a compressor 8 and then conducted by pipe 9 to a feed manifold 10 from which a part may be forced into the inlet of coil 1 by line 11 and the remainder introduced directly into drum 3 by line 12.
- the drum is preferably protected against excessive loss of heat as by insulation 13.
- Vapor from drum 3 is conducted by vapor line 14 to a heat exchanger 15, then to a condenser 16 and gas separator 17. Distillate is conducted to storage (not shown) by pipe 17' while gas is recompressed by booster pump 18 and returned to hydrogen manifold 10 by pipe 18'. The gas may be purified before return to the manifold,
- a part of the oily mass undergoing treatr n ent is withdrawn from drum 3, preferably in a continuous stream, by a line 19 which is fitted with a pressure reduction valve 20 and is discharged into a chamber 21.
- Chamber 21 may be of any suitable form, with or without ba flles 22, but with a lower chamber 23 which is furnished with a double bell closure 23' or. other suitable means for discharging solid or semi-solid materials intermittently.
- a vapor pipe 24 conducts vaporized oil to condenser 25 and discharges it into 'a separator 26 from which gas is removed, by vacuum pump 28. Condensate is withdrawn from separator 26 by pump 29 and is returned to drum 4 as will be described below.
- a current of inert gas may be passed into drum 21 by pipe 21a in order to assist in the vaporization of the liquid after reduction of pressure.
- Fresh oil is drawn from storage (not shown) by pump 31 and a part may be diverted through a pulverizer 32 in which coal or other solid carbonaceous material is reduced to a finely divided state and thoroughly incorporated with the oil.
- Condensate from drum 26 is forced by pump 29 through a line 30 into a branch pipe so that it may be passed through pulverizer 32 or may be added to the mixture of oil and coal as shown in the drawing. In any case the mixture is then forced through heat exchanger 15 to coil 1 by line 34.
- crude oils, tar and the like may be used as the base and carbonaceous material which contains ash or other foreign solid impurities is suspended in the oily liquid.
- Such material is subjected to the action of a gas rich in free hydrogen under a high pressure, for example, above about 25 atmospheres and preferably at 100 or 200 atmospheres or higher.
- the body of material which is in a semiliquid, at least pumpable form, is maintained at a temperature within the approximate range of 750 to 850 degrees Fahrenheit. Hydrogen is continuously forced into the body of oily material and vapor which comprises distillate and gas is continuously removed during the hydrogenation.
- Part of the oily mixture is withdrawn from drum 3 and discharged into a chamber 21 which is. maintained at a pressure considerably lower than drum 3.
- a large part of the oil withdrawn is vaporized and separated from solid matter, such as ash, free carbon, unvaporlzable asphaltic residue, and the like.
- the distillation is preferably done under vacuum and the 100 solid matter may be obtained in substantially dry form, at least, freed from the majority of the oil which is condensed and preferably returned to the body of material undergoing hydrogenation in drum 3.
- coil 1 may be used merely 110- as a preheating coil for the fresh suspension of carbonaceous material in oil. It will be understood that, if desired, fresh oil need not be continuously supplied; but after the cycle has been established, heavy oil may be produced in sufficient quantity to furnish the suspension medium for the entire quantity of coal or other carbonaceous material heated.
- An improved process for production of low boiling liquid hydrocarbons from solid carbonaceous materials comprising, forming a suspension of finely ground carbonaceous material in heavy oil, maintaining a body of the suspension at a decomposition temperature and under high pressure, continuously forcing a hot mixture of the suspension and a gas rich in free hydrogen into the body, continuously withdrawing vapor therefrom, condensing low boiling liquid hydrocarbon from the vapor, separately withdrawing a part of the suspension from the body, reducing pressure on the part thus withdrawn whereby substantially all of the oil is vaporized, condensing the vapor and returning a part of the condensate to the body of the material undergoing treatment.
- An improved process for producing valuable liquid hydrocarbons from solid carbonaceous material which comprises reducing such material to a finely divide'd state, suspending the same in heavy hydrocarbon oil, maintaining a body of such suspension at an elevated temperature and under high pressure in contact with a gas rich in free hydrogen, continuously removing vapors from the body of suspension, separately withdrawing a part of the suspension from the body, reducing pressure on the part withdrawn whereby a substantial portion of the hydrocarbon liquid is vaporized, passing a current of inert gas through the residue after reduction of pressure, and separately condensing the vapor evolved by the reduction of pressure.
- An improved process for producing liquid hydrocarbons from solid carbonaceous material 100 which comprises reducing such material to a finely divided state, suspending the same in heavy hydrocarbon oil, subjecting a body of such suspension to the action of a gas rich in free hydrogen at an elevated temperature and under 105 high pressure, continuously removing vapors from the body of suspension, separately withdrawing a portion of the suspension from the mass undergoing hydrogenation, reducing pressure on the portion withdrawn to a sub-atmospheric pres- 110 sure whereby a substantial portion of the hydrocarbon liquid is vaporized, and separately eondensing the vapor.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
Dec. 19, 1933. R. P. RUSSELL 1,940,648
PROCESS FOR OBTAINING VALUABLE DISTILLATES FROM CARBONACEOUS MATERIALS Filed Jan. 22, 1929 $7M 0. M Svwemtoz J Patented Dec. 19, 1933 PATENT OFFICE PROCESS FOR OBTAINING VALUABLE DISTILLATES F R O M CARBONACEOUS MATERIALS Robert P. Russell, Baton Rouge, La., assignor to Standard-I. G. Company Application January 22, 1929. Serial No. 334,148
' Claims.
The present invention comprises an improved process for obtaining valuable low boiling oils from carbonaceous materials such as petroleum, tars and the like and also from solid carbona- 5 ceous materials especially those, which like coal, contain solid foreign matter. My process will be fully understood from the following description and the drawing.
The drawing is a semi-diagrammatic view in sectionalzelevation of an apparatus constructed according to my invention and indicates the fiow of materials.
Referring to the drawing, reference numeral 1 denotes a pipe coil arranged in a suitablefurnace setting 2 and adapted to heat a stream of hydrocarbon oil or the like to an elevated temperature. The coil discharges into a reaction chamber 3 which is constructed to withstand high internal pressure and high temperature,
as well as the corrosive eifects of the reactants.
The contents of the drum is kept in thorough agitation by means of a stirrer 4 or the like and the temperature of the drum is maintained at the desired level in any suitable manner, for example, by the use of internal electrical heaters. but I prefer to continuously withdraw apart of the oil by pipe 5 and circulate the same by means of a suitable pump 6 back to drum 3 by way of coil 1. Hydrogen or a gas rich in free hydrogen is withdrawn from a suitable source (not shown) by pipe 7, compressed by a compressor 8 and then conducted by pipe 9 to a feed manifold 10 from which a part may be forced into the inlet of coil 1 by line 11 and the remainder introduced directly into drum 3 by line 12. The drum is preferably protected against excessive loss of heat as by insulation 13.
Vapor from drum 3 is conducted by vapor line 14 to a heat exchanger 15, then to a condenser 16 and gas separator 17. Distillate is conducted to storage (not shown) by pipe 17' while gas is recompressed by booster pump 18 and returned to hydrogen manifold 10 by pipe 18'. The gas may be purified before return to the manifold,
for example, by washing with an aqueous soda solution to remove hydrogen sulphide and then with oil to remove gaseous hydrocarbons.
A part of the oily mass undergoing treatr n ent is withdrawn from drum 3, preferably in a continuous stream, by a line 19 which is fitted with a pressure reduction valve 20 and is discharged into a chamber 21. Chamber 21 may be of any suitable form, with or without ba flles 22, but with a lower chamber 23 which is furnished with a double bell closure 23' or. other suitable means for discharging solid or semi-solid materials intermittently. A vapor pipe 24 conducts vaporized oil to condenser 25 and discharges it into 'a separator 26 from which gas is removed, by vacuum pump 28. Condensate is withdrawn from separator 26 by pump 29 and is returned to drum 4 as will be described below. A current of inert gas may be passed into drum 21 by pipe 21a in order to assist in the vaporization of the liquid after reduction of pressure.
Fresh oil is drawn from storage (not shown) by pump 31 and a part may be diverted through a pulverizer 32 in which coal or other solid carbonaceous material is reduced to a finely divided state and thoroughly incorporated with the oil. Condensate from drum 26 is forced by pump 29 through a line 30 into a branch pipe so that it may be passed through pulverizer 32 or may be added to the mixture of oil and coal as shown in the drawing. In any case the mixture is then forced through heat exchanger 15 to coil 1 by line 34.
In the operation of my process, crude oils, tar and the like may be used as the base and carbonaceous material which contains ash or other foreign solid impurities is suspended in the oily liquid. Such material is subjected to the action of a gas rich in free hydrogen under a high pressure, for example, above about 25 atmospheres and preferably at 100 or 200 atmospheres or higher. The body of material which is in a semiliquid, at least pumpable form, is maintained at a temperature within the approximate range of 750 to 850 degrees Fahrenheit. Hydrogen is continuously forced into the body of oily material and vapor which comprises distillate and gas is continuously removed during the hydrogenation.
Part of the oily mixture is withdrawn from drum 3 and discharged into a chamber 21 which is. maintained at a pressure considerably lower than drum 3. By this means, a large part of the oil withdrawn is vaporized and separated from solid matter, such as ash, free carbon, unvaporlzable asphaltic residue, and the like. The distillation is preferably done under vacuum and the 100 solid matter may be obtained in substantially dry form, at least, freed from the majority of the oil which is condensed and preferably returned to the body of material undergoing hydrogenation in drum 3.
When a relatively large proportion of coal is used with the oil, the reaction is strongly exothermic and furnishes sufflcient' heat to maintain temperature in the'drum without internal heating or the like, and coil 1 may be used merely 110- as a preheating coil for the fresh suspension of carbonaceous material in oil. It will be understood that, if desired, fresh oil need not be continuously supplied; but after the cycle has been established, heavy oil may be produced in sufficient quantity to furnish the suspension medium for the entire quantity of coal or other carbonaceous material heated.
My invention is not to be limited by any theory of the process, nor by merely an illustrative example, but only by the following claims-in which I wish to claim all novelty inherent in the invention. a
I claim:
1. An improved process for production of low boiling liquid hydrocarbons from solid carbonaceous materials comprising, forming a suspension of finely ground carbonaceous material in heavy oil, maintaining a body of the suspension at a decomposition temperature and under high pressure, continuously forcing a hot mixture of the suspension and a gas rich in free hydrogen into the body, continuously withdrawing vapor therefrom, condensing low boiling liquid hydrocarbon from the vapor, separately withdrawing a part of the suspension from the body, reducing pressure on the part thus withdrawn whereby substantially all of the oil is vaporized, condensing the vapor and returning a part of the condensate to the body of the material undergoing treatment.
2. Process according to claim 1 in which the suspension of solid material in oil is maintained at a temperature of approximately 750-850 degrees Fahrenheit and under pressure in excess of 25 atmospheres.
3. In a process for the liquefaction of coal the steps of maintaining a body of finely divided coal suspended in heavy oil at high temperature and 7 under high pressure of hydrogen, continuously removing the vapors evolved therefrom, separately withdrawing a part of the suspension containing ash, reducing pressure on the part withdrawn whereby the liquid is substantially completely vaporized, separately condensing this vapor and returning the condensate to the, body of coal and oil.
4. An improved process for producing valuable liquid hydrocarbons from solid carbonaceous material which comprises reducing such material to a finely divide'd state, suspending the same in heavy hydrocarbon oil, maintaining a body of such suspension at an elevated temperature and under high pressure in contact with a gas rich in free hydrogen, continuously removing vapors from the body of suspension, separately withdrawing a part of the suspension from the body, reducing pressure on the part withdrawn whereby a substantial portion of the hydrocarbon liquid is vaporized, passing a current of inert gas through the residue after reduction of pressure, and separately condensing the vapor evolved by the reduction of pressure.
5. An improved process for producing liquid hydrocarbons from solid carbonaceous material 100 which comprises reducing such material to a finely divided state, suspending the same in heavy hydrocarbon oil, subjecting a body of such suspension to the action of a gas rich in free hydrogen at an elevated temperature and under 105 high pressure, continuously removing vapors from the body of suspension, separately withdrawing a portion of the suspension from the mass undergoing hydrogenation, reducing pressure on the portion withdrawn to a sub-atmospheric pres- 110 sure whereby a substantial portion of the hydrocarbon liquid is vaporized, and separately eondensing the vapor.
ROBERT P. RUSSELL.
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NL29952D NL29952C (en) | 1929-01-22 | ||
US334148A US1940648A (en) | 1929-01-22 | 1929-01-22 | Process for obtaining valuable distillates from carbonaceous materials |
FR687415D FR687415A (en) | 1929-01-22 | 1929-12-30 | Process for producing valuable distillates using carbonaceous materials |
GB2085/30A GB340811A (en) | 1929-01-22 | 1930-01-21 | An improved process for obtaining valuable distillates by the destructive hydrogenation of carbonaceous materials |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US334148A US1940648A (en) | 1929-01-22 | 1929-01-22 | Process for obtaining valuable distillates from carbonaceous materials |
Publications (1)
Publication Number | Publication Date |
---|---|
US1940648A true US1940648A (en) | 1933-12-19 |
Family
ID=23305806
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US334148A Expired - Lifetime US1940648A (en) | 1929-01-22 | 1929-01-22 | Process for obtaining valuable distillates from carbonaceous materials |
Country Status (4)
Country | Link |
---|---|
US (1) | US1940648A (en) |
FR (1) | FR687415A (en) |
GB (1) | GB340811A (en) |
NL (1) | NL29952C (en) |
Cited By (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2453641A (en) * | 1944-02-05 | 1948-11-09 | Lummus Co | Method of producing colloidal fuel |
US3477941A (en) * | 1968-01-25 | 1969-11-11 | Universal Oil Prod Co | Method of treating coal |
US3503864A (en) * | 1967-12-29 | 1970-03-31 | Universal Oil Prod Co | Coal liquefaction method |
US3505202A (en) * | 1967-06-26 | 1970-04-07 | Universal Oil Prod Co | Solvent extraction method |
US3505203A (en) * | 1967-06-26 | 1970-04-07 | Universal Oil Prod Co | Solvent extraction method |
EP0027962A2 (en) * | 1979-10-27 | 1981-05-06 | BASF Aktiengesellschaft | Process for the production of liquid hydrocarbons from coal |
WO1982000655A1 (en) * | 1980-08-26 | 1982-03-04 | Duraiswamy K | Pyrolysis process |
US4324639A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process with feed pretreatment |
US4324637A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process with feed pretreatment utilizing a beneficially reactive gas |
US4324638A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for stabilizing volatile hydrocarbons |
US4324644A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for stabilizing volatile hydrocarbons utilizing a beneficially reactive gas |
US4324642A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for producing condensed stabilized hydrocarbons utilizing a beneficially reactive gas |
US4324640A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process |
US4324641A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process utilizing a beneficially reactive gas |
US5100536A (en) * | 1989-04-28 | 1992-03-31 | Ruhrkohle Ag | Method of processing substances |
-
0
- NL NL29952D patent/NL29952C/xx active
-
1929
- 1929-01-22 US US334148A patent/US1940648A/en not_active Expired - Lifetime
- 1929-12-30 FR FR687415D patent/FR687415A/en not_active Expired
-
1930
- 1930-01-21 GB GB2085/30A patent/GB340811A/en not_active Expired
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2453641A (en) * | 1944-02-05 | 1948-11-09 | Lummus Co | Method of producing colloidal fuel |
US3505202A (en) * | 1967-06-26 | 1970-04-07 | Universal Oil Prod Co | Solvent extraction method |
US3505203A (en) * | 1967-06-26 | 1970-04-07 | Universal Oil Prod Co | Solvent extraction method |
US3503864A (en) * | 1967-12-29 | 1970-03-31 | Universal Oil Prod Co | Coal liquefaction method |
US3477941A (en) * | 1968-01-25 | 1969-11-11 | Universal Oil Prod Co | Method of treating coal |
EP0027962A2 (en) * | 1979-10-27 | 1981-05-06 | BASF Aktiengesellschaft | Process for the production of liquid hydrocarbons from coal |
EP0027962A3 (en) * | 1979-10-27 | 1981-11-11 | Basf Aktiengesellschaft | Process for the production of liquid hydrocarbons from coal |
US4324639A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process with feed pretreatment |
WO1982000655A1 (en) * | 1980-08-26 | 1982-03-04 | Duraiswamy K | Pyrolysis process |
US4324637A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process with feed pretreatment utilizing a beneficially reactive gas |
US4324638A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for stabilizing volatile hydrocarbons |
US4324644A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for stabilizing volatile hydrocarbons utilizing a beneficially reactive gas |
US4324642A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for producing condensed stabilized hydrocarbons utilizing a beneficially reactive gas |
US4324640A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process |
US4324643A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process for producing condensed stabilized hydrocarbons |
US4324641A (en) * | 1980-08-26 | 1982-04-13 | Occidental Research Corporation | Pyrolysis process utilizing a beneficially reactive gas |
US5100536A (en) * | 1989-04-28 | 1992-03-31 | Ruhrkohle Ag | Method of processing substances |
Also Published As
Publication number | Publication date |
---|---|
NL29952C (en) | |
FR687415A (en) | 1930-08-08 |
GB340811A (en) | 1931-01-08 |
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