US3576734A - Process for production of synthetic crude oil from low temperature coal tars - Google Patents
Process for production of synthetic crude oil from low temperature coal tars Download PDFInfo
- Publication number
- US3576734A US3576734A US762611A US3576734DA US3576734A US 3576734 A US3576734 A US 3576734A US 762611 A US762611 A US 762611A US 3576734D A US3576734D A US 3576734DA US 3576734 A US3576734 A US 3576734A
- Authority
- US
- United States
- Prior art keywords
- low temperature
- crude oil
- synthetic crude
- tars
- production
- 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
Links
- 239000011269 tar Substances 0.000 title abstract description 18
- 238000000034 method Methods 0.000 title abstract description 15
- 239000010779 crude oil Substances 0.000 title abstract description 14
- 239000003245 coal Substances 0.000 title abstract description 8
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- 239000000463 material Substances 0.000 abstract description 8
- 238000003763 carbonization Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 13
- 229910052739 hydrogen Inorganic materials 0.000 description 12
- 239000001257 hydrogen Substances 0.000 description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 10
- 239000000047 product Substances 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 229910017464 nitrogen compound Inorganic materials 0.000 description 4
- 150000002830 nitrogen compounds Chemical class 0.000 description 4
- 239000002802 bituminous coal Substances 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 239000011287 low-temperature tar Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 150000007513 acids Chemical class 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000011800 void material Substances 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000029936 alkylation Effects 0.000 description 1
- 238000005804 alkylation reaction Methods 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006698 induction Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- -1 parafiins Chemical class 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000004525 petroleum distillation Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
Classifications
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
-
- 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
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
Definitions
- This invention relates to an improved process for the economical production of synthetic crude oil.
- the synthetic crude oil is obtained from low temperature coal tars which have been obtained by carefully controlling the temperature during the carbonization of various cool materials such as coal.
- the synthetic crude oil and accompanying gaseous products are obtained by introducing heated low temperature tars with hydrogen into an insulated drum containing a suitable catalyst comprising one or more of the following elements: cobalt, molybdenum or nickel.
- a suitable catalyst comprising one or more of the following elements: cobalt, molybdenum or nickel.
- the residence time of the combined heated low temperature tars and hydrogen in the presence of the catalyst is sufiicient to produce a petroleum-like synthetic crude oil.
- a batch or continuous type process may be used to accomplish the formation of an expanded high-type" synthetic crude oil.
- This expanded high grade synthetic crude oil from which most of the fixed or organic sulphur has been removed during the process contains a large percentage of naphtha and is ready for further processing.
- the bottoms product or remainder of the synthetic crude can be introduced as a recycle into the low temperature tars entering the system.
- the synthetic crude oil formed by the process of the present invention can be refined by any of the processes well known in the petroleum industry. End products after refining, deepnding on the variation of heat, pressure and time that the low temperature tars and hydrogen are in contact with the catalyst will contain high percentages of aromatic hydrocarbons, amines, phenols, parafiins, olefins and various other light end materials. Gaseous products formed will contain hydrogen, light end gases, nitrogen compounds, and hydrogen sulfide, all of which can be processed into marketable products.
- carbonaceous material such as bituminous coal and the like
- a suitable roaster such as multi-hearth vertical roaster, under controlled temperature with the gases removed at each level to avoid overheating.
- the solid material is retained in the roaster from two to four hours at a temperature of from between 400 to 600 centigrade.
- the rotation speed of the roaster arms and the feed is regulated to assure the desired retention time.
- the roaster arms preferably move the material along with a plowtype action.
- the roaster preferably has a heat exchange and induction center at the bottom thereof for the introduction of the super heated steam. The exhaust resulting This exhaust is treated to separate the hydrogen and carbon materials and the hydrogen is retained for subsequent use.
- the hot distillation gases emitted at the various levels of the roaster are cleaned and condensed into low temperature tars with the remaining gases sent to the light end plant.
- approximately 1200 to 1500 cubic feet of hydrogen is added to each barrel of low temperature tar and salvaged bottoms and the mixture is brought into contact with a fixed bed catalyst under controlled pressure, heat and time.
- a single autoclave-type batch unit having a void to catalyst ratio of from 1:1 to 4:1 can be advantageously used, or a continuous flow through unit with a liquid hourly space velocity (oil-to-catalyst volume ratio) of from 1.5 to 4.0 can be used.
- the pressure in the units is maintained from between 700 to 2000 p.s.i., and the temperature is maintained between 350 to 500 C.
- the tars are passed through a primary reactor at a temperature between 350-370 C., and are then passed through a second reactor at a temperature of from 450 to 490 C.
- the resulting effiuent is then cooled into synthetic crude oil and gases. After cooling, the gases con taining hydrogen sulfide, hydrogen, various light end hydrocarbons and nitrogen compounds are removed and further processed.
- the hydrogen gas can be recycled and introduced into the low temperature tar stream entering the reaction chamber or burned as a flare gas.
- the hydrogen sulphides can be processed to produce a commercial sulphur or processed with hydrogen to produce commercial acids.
- the light hydrocarbons can further be refined in light end units where yielded off-gases are erturned for production heat.
- the nitrogen compounds can be converted into commercial fertilizer, acids and other products.
- the low temperature tar which has been converted into a synthetic crude stock is then processed in a conventional petroleum distillation unit to yield a naphtha product boiling below 250 C. and a series of gases which are utilized in light ends plant or burned as excess.
- the synthetic crude after removal of the naphtha and light end gases becomes residual and can be recycled with low temperature tars or further treated to form various grades of asphaltic material, fuel oils and lubricating stock.
- the material removed from the distillation unit as a naphtha out can be further procesed into regular petroleum products or petrochemicals utilizing any number of refining processes known to the art.
- the light ends plant consist of polymerization, alkylation and/or isomerization units.
- the phenols can also be processed into commercial units.
- a process for preparing an allely sulfur free synthetic crude oil which comprises the steps of:
- bituminous coal is roasted at about 400 to 600 C. in the presence of steam.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A PROCESS FOR THE PRODUCTION OF SYNTHETIC CRUDE OIL FROM LOW TEMPERATURE COAL TARS WHICH HAVE BEEN OBTAINED BY CAREFUL TEMPERATURE CONTROL DURING THE CARBONIZATION OF VARIOUS COOL MATERIALS, SUCH AS COAL.
Description
United States Patent Ollice 3,576,734 Patented Apr. 27, 1971 3,576,734 PROCESS FOR PRODUCTION OF SYNTHETIC CRUDE OIL FROM LOW TEMPERATURE COAL TARS Harold L. Bennett, Indianapolis, Ind., assignor to Bennett Engineering Company, Rnshville, Ind. No Drawing. Filed Sept. 25, 1968, Ser. No. 762,611 Int. Cl. C10g N US. Cl. 208-8 Claims ABSTRACT OF THE DISCLOSURE A process for the production of synthetic crude oil from low temperature coal tars which have been obtained by careful temperature control during the carbonization of various cool materials, such as coal.
SUMMARY OF THE INVENTION This invention relates to an improved process for the economical production of synthetic crude oil. The synthetic crude oil is obtained from low temperature coal tars which have been obtained by carefully controlling the temperature during the carbonization of various cool materials such as coal.
Generally speaking the synthetic crude oil and accompanying gaseous products are obtained by introducing heated low temperature tars with hydrogen into an insulated drum containing a suitable catalyst comprising one or more of the following elements: cobalt, molybdenum or nickel. The residence time of the combined heated low temperature tars and hydrogen in the presence of the catalyst is sufiicient to produce a petroleum-like synthetic crude oil. A batch or continuous type process may be used to accomplish the formation of an expanded high-type" synthetic crude oil. This expanded high grade synthetic crude oil from which most of the fixed or organic sulphur has been removed during the process contains a large percentage of naphtha and is ready for further processing. Following removal of the naphtha fractions by methods well known in the art, the bottoms product or remainder of the synthetic crude can be introduced as a recycle into the low temperature tars entering the system.
The synthetic crude oil formed by the process of the present invention can be refined by any of the processes well known in the petroleum industry. End products after refining, deepnding on the variation of heat, pressure and time that the low temperature tars and hydrogen are in contact with the catalyst will contain high percentages of aromatic hydrocarbons, amines, phenols, parafiins, olefins and various other light end materials. Gaseous products formed will contain hydrogen, light end gases, nitrogen compounds, and hydrogen sulfide, all of which can be processed into marketable products.
DESCRIPTION OF THE PREFERRED EMBODIMENT In the practice of the present invention carbonaceous material, such as bituminous coal and the like, is introduced into a suitable roaster, such as multi-hearth vertical roaster, under controlled temperature with the gases removed at each level to avoid overheating. The solid material is retained in the roaster from two to four hours at a temperature of from between 400 to 600 centigrade. The rotation speed of the roaster arms and the feed is regulated to assure the desired retention time. The roaster arms preferably move the material along with a plowtype action. The roaster preferably has a heat exchange and induction center at the bottom thereof for the introduction of the super heated steam. The exhaust resulting This exhaust is treated to separate the hydrogen and carbon materials and the hydrogen is retained for subsequent use.
After the hot gases have been removed the remaining soild material, high volatile char, are removed mechanically from the roaster, cooled, and marketed or further processed into producer gas which in turn is marketed for heating or refined into light end products.
The hot distillation gases emitted at the various levels of the roaster are cleaned and condensed into low temperature tars with the remaining gases sent to the light end plant. At this point approximately 1200 to 1500 cubic feet of hydrogen is added to each barrel of low temperature tar and salvaged bottoms and the mixture is brought into contact with a fixed bed catalyst under controlled pressure, heat and time. A single autoclave-type batch unit having a void to catalyst ratio of from 1:1 to 4:1 can be advantageously used, or a continuous flow through unit with a liquid hourly space velocity (oil-to-catalyst volume ratio) of from 1.5 to 4.0 can be used. The pressure in the units is maintained from between 700 to 2000 p.s.i., and the temperature is maintained between 350 to 500 C. Generally, the tars are passed through a primary reactor at a temperature between 350-370 C., and are then passed through a second reactor at a temperature of from 450 to 490 C. The resulting effiuent is then cooled into synthetic crude oil and gases. After cooling, the gases con taining hydrogen sulfide, hydrogen, various light end hydrocarbons and nitrogen compounds are removed and further processed.
The hydrogen gas can be recycled and introduced into the low temperature tar stream entering the reaction chamber or burned as a flare gas. The hydrogen sulphides can be processed to produce a commercial sulphur or processed with hydrogen to produce commercial acids. The light hydrocarbons can further be refined in light end units where yielded off-gases are erturned for production heat. The nitrogen compounds can be converted into commercial fertilizer, acids and other products.
The low temperature tar which has been converted into a synthetic crude stock is then processed in a conventional petroleum distillation unit to yield a naphtha product boiling below 250 C. and a series of gases which are utilized in light ends plant or burned as excess. The synthetic crude after removal of the naphtha and light end gases becomes residual and can be recycled with low temperature tars or further treated to form various grades of asphaltic material, fuel oils and lubricating stock.
The material removed from the distillation unit as a naphtha out can be further procesed into regular petroleum products or petrochemicals utilizing any number of refining processes known to the art. The light ends plant consist of polymerization, alkylation and/or isomerization units. The phenols can also be processed into commercial units.
The invention claimed is:
1. A process for preparing an esentially sulfur free synthetic crude oil which comprises the steps of:
(a) Roasting bituminous coal at a temperature of about 400 to 600 C. for about '2 to 4 hours,
(b) Continuously collecting and condensing the distillation gases,
(c) Separating the low temperature tars from the condensed gaseous products.
(d) Contacting the low temperature tars with a cobaltmolybdenum catalyst in a fixed bed system heated to a temperature of 350 to 500 C. and a pressure of 700 to 200 p.s.i. in the presence of hydrogen added in an amount equal to 1200 to 1500 cubic feet of hydrogen per barrel of low temperature tars,
(e) Cooling the efliuent from the reactor and separating the gaseous products containing hydrogen, hydrogen sulfide and nitrogen compounds therefrom and (f) Recovering the essentially sulfur free synthetic crude oil product.
2. A process according to claim 1 wherein the low temperature tars are fed into a primary reactor maintained at a temperature of 350 to 370 C. and then passed thru a second reactor heated to a temperature of 450 to 490 C.
3. The process according to claim 1 wherein the low temperature tars are contacted in an autoclave unit with a void space to catalyst ratio of 1:1 to 4: 1.
4. The process according to claim 1 wherein the low temperature tars are contacted in a continuous flow thru unit at a weight hourly space velocity of 1.5 to 4.0.
5. The process according to claim 1 wherein the bituminous coal is roasted at about 400 to 600 C. in the presence of steam.
References Cited UNITED STATES PATENTS 1,879,750 9/1932 Joseph 208-8 10 1,702,899 2/1929 Howard 208-8 1,954,096 4/1934 Pier 2088 DELBERT E. GANTZ, Primary Examiner 15 V. OKEEFE, Assistant Examiner
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US76261168A | 1968-09-25 | 1968-09-25 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US3576734A true US3576734A (en) | 1971-04-27 |
Family
ID=25065571
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US762611A Expired - Lifetime US3576734A (en) | 1968-09-25 | 1968-09-25 | Process for production of synthetic crude oil from low temperature coal tars |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US3576734A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3839186A (en) * | 1973-07-02 | 1974-10-01 | Universal Oil Prod Co | Process for producing volatile hydrocarbon products from coal and hydrogen |
| US3960700A (en) * | 1975-01-13 | 1976-06-01 | Cities Service Company | Coal hydrogenation to produce liquids |
| US4239705A (en) * | 1979-05-25 | 1980-12-16 | Gulf Research & Development Company | Process for producing acetaldehyde |
| US4273643A (en) * | 1979-10-01 | 1981-06-16 | Bennett Engineering Inc. | Process for production of synthetic crude oil, alcohols, and chars during low temperature carbonization of coals |
| US7909896B2 (en) | 2001-11-27 | 2011-03-22 | Bennett Engineers and Associates of Austin Colorado | Process for production of low temperature char during production of low temperature tars |
-
1968
- 1968-09-25 US US762611A patent/US3576734A/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3839186A (en) * | 1973-07-02 | 1974-10-01 | Universal Oil Prod Co | Process for producing volatile hydrocarbon products from coal and hydrogen |
| US3960700A (en) * | 1975-01-13 | 1976-06-01 | Cities Service Company | Coal hydrogenation to produce liquids |
| US4239705A (en) * | 1979-05-25 | 1980-12-16 | Gulf Research & Development Company | Process for producing acetaldehyde |
| US4273643A (en) * | 1979-10-01 | 1981-06-16 | Bennett Engineering Inc. | Process for production of synthetic crude oil, alcohols, and chars during low temperature carbonization of coals |
| US7909896B2 (en) | 2001-11-27 | 2011-03-22 | Bennett Engineers and Associates of Austin Colorado | Process for production of low temperature char during production of low temperature tars |
| US20110131872A1 (en) * | 2001-11-27 | 2011-06-09 | Bennett Harold L | Process for production of low temperature char during production of low temperature tars |
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