US2001444A - Process of refining oils and the like by steam treatment - Google Patents
Process of refining oils and the like by steam treatment Download PDFInfo
- Publication number
- US2001444A US2001444A US548427A US54842731A US2001444A US 2001444 A US2001444 A US 2001444A US 548427 A US548427 A US 548427A US 54842731 A US54842731 A US 54842731A US 2001444 A US2001444 A US 2001444A
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- US
- United States
- Prior art keywords
- steam
- pressure
- heat
- steam treatment
- vessel
- 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
- 238000000034 method Methods 0.000 title description 14
- 239000003921 oil Substances 0.000 title description 11
- 238000007670 refining Methods 0.000 title description 2
- 238000006243 chemical reaction Methods 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000000463 material Substances 0.000 description 6
- 238000005336 cracking Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000000717 retained effect Effects 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000000887 hydrating effect Effects 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000011279 mineral tar Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004326 stimulated echo acquisition mode for imaging Methods 0.000 description 1
- 235000010269 sulphur dioxide Nutrition 0.000 description 1
- 239000004291 sulphur dioxide Substances 0.000 description 1
- 239000002641 tar oil Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Images
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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
- C10C1/00—Working-up tar
- C10C1/20—Refining by chemical means inorganic or organic compounds
-
- 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
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
- C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
- C10G9/38—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours produced by partial combustion of the material to be cracked or by combustion of another hydrocarbon
Definitions
- steam is gener-v ated at a pressure of about 200 atmospheres and superheated to a temperature of about 500 C.
- This steam is employed, for instance for the cracking of heavy oils, the heat being transferred to the latter.
- the transference of heat can be effected up to the saturation temperature, in this case about 364 C.
- the hot water under pressure can be employed in a heat exchanger for preheating the fresh water used for the steam generation, the entire heat being thereby recovered.
- the condensate can be returned to the steam generator for renewed conversion into steam.
- the condensation of the steam during the process can be effected in various manners, for instance by the preheating of materials with the steam or by dephlegmation, cooling or the like according to the result aimed at.
- the device comprises a reaction chamber I wherein the materials, for instance heavy oils, are treated by direct heat interchange with steam produced in a generator 2 at a pressure of about 200 atmospheres and superheated to about 500 C.
- This steam after having transferred its excess heat to the materials, is led into a second, upright pressure vessel 3 wherein oil is treated by the steam before it is fed into the chamber I.
- the steam is condensed, and the condensate, still under pressure, is collected at the bottom 4 of the vessel.
- the oil is mostly incapable of mixing with the water and forms, on the surface of the latter, a layer 5 whence it can be fed into the chamber I.
- the hot condensate under pressure is fed into an intermediary collector 6 whence it can be returnedjby means of a pump H into the generator 2 for renewed conversicninto'ste'am; Alternately; the highly heated water can be passed through a heat exchanger vessel 7 for preheating fresh water fed by means of a pump 8 from a tank 9 into the steam generator'2.
- the oil in the dephlegmator acquires a temperature which renders its decomposition in the reaction chamber by the superheated steam ex- 10 tremely'" easy.
- This favourable temperature is obtained owing to the high pressure of the steam.
- the pressure may be lowered somewhat, andthe oil may be retained for a longer period in the dephlegmator than in the reaction chamber if a particularly refined product is. aimed at.
- the pressure For rapid cracking, however, the oil is retained for a longer period in the reaction chamber.
- the pressure must be as high as possible, the Work being carried on with an excess of steam as compared with the oil.
- the water soluble substances contained in the materials and carried away with the condensate are removed from the latter before its re-introduction into the steam generator 2.
- This can be eifected in a vessel l4 in known manner, for instance by lixiviation with suitable known reagents capable of dissolving the phenols and oxides or by a fractional cooling in which the oil is automatically disengaged.
- This treatment of the Favourable combinations of reaction chamber I by throttling the steam at I2, in which case a pump 13 must be used for feeding the oil from the vessel 3 into the chamber l, or part of the cold water under pressure may, for condensing the steam in the vessel 3, be
- Coal paste may be treated together with hydrogen containing materials for liquefaction, and hydrocarbons and tar oils may be refined in this manner.
- Various hydration processes can be carried out in this manner, in which case the steamis used not only as a heating medium but also as a reagent in known manner.
- the employment of the highly superheated steam according to the present invention does not exclude thesimultaneous use of difi'erent, chemically acting gases and vapours such as air, oxygen, hydrogen, carbon oxide, ammonia, sulphur dioxide and the like which may be introduced together with the steam through a pipe I 5.
- gases and vapours such as air, oxygen, hydrogen, carbon oxide, ammonia, sulphur dioxide and the like which may be introduced together with the steam through a pipe I 5.
- the time of reaction is determined, as is usual in the art, by the nature of the raw material under treatment.
- the process according to the invention has many technical advantages. By the employment of superheated steam a large yield of heat can be obtained from camparatively small apparatus, and the saving of heat by carrying out the process according to the present invention is considerable.
- a process of cracking mineral tar oils and similar substances comprising feeding the initial substance through a dephlegmating zone into a reaction zone, generating steam at a pressure of about 200 atmospheres, feeding said steam at such pressure and at a temperature of about 500 C. through the reaction zone into the dephlegmating zone, condensing the major portion of the steam in .the dephlegmating zone into water under pressure, and utilizing said water under pressure in the steam generation.
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)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
Patented May 14, 1935 UNITED smrss PRocEs's' F REFINING oiLs AND THE LIKE BY STEAM TREATMENT Georg Zotos, Gharlottenburg, Germany Application July 2, 1931,, Serial No. 548,427
In Germany March 3 1930 V 3 Claims.
In carrying out the process, steam is gener-v ated at a pressure of about 200 atmospheres and superheated to a temperature of about 500 C. This steam is employed, for instance for the cracking of heavy oils, the heat being transferred to the latter. Owing to the high pressure, the transference of heat can be effected up to the saturation temperature, in this case about 364 C. At this comparatively high temperature it is possible to utilize most if not all of the heat of vaporization in the process itself so as to convert the steam into hot condensate which can easily be withdrawn from the apparatus. The hot water under pressure can be employed in a heat exchanger for preheating the fresh water used for the steam generation, the entire heat being thereby recovered. Alternately the condensate can be returned to the steam generator for renewed conversion into steam.
The condensation of the steam during the process can be effected in various manners, for instance by the preheating of materials with the steam or by dephlegmation, cooling or the like according to the result aimed at.
The invention is illustrated in the accompanying drawing which represents a diagrammatic view of an apparatus whereby the process can be carried out.
The device comprises a reaction chamber I wherein the materials, for instance heavy oils, are treated by direct heat interchange with steam produced in a generator 2 at a pressure of about 200 atmospheres and superheated to about 500 C. This steam, after having transferred its excess heat to the materials, is led into a second, upright pressure vessel 3 wherein oil is treated by the steam before it is fed into the chamber I. By the further transfer of heat in the vessel 3, the steam is condensed, and the condensate, still under pressure, is collected at the bottom 4 of the vessel. The oil is mostly incapable of mixing with the water and forms, on the surface of the latter, a layer 5 whence it can be fed into the chamber I. The hot condensate under pressure is fed into an intermediary collector 6 whence it can be returnedjby means of a pump H into the generator 2 for renewed conversicninto'ste'am; Alternately; the highly heated water can be passed through a heat exchanger vessel 7 for preheating fresh water fed by means of a pump 8 from a tank 9 into the steam generator'2.
Under the influence of the condensing steam, the oil in the dephlegmator acquires a temperature which renders its decomposition in the reaction chamber by the superheated steam ex- 10 tremely'" easy. This favourable temperature is obtained owing to the high pressure of the steam. The pressure may be lowered somewhat, andthe oil may be retained for a longer period in the dephlegmator than in the reaction chamber if a particularly refined product is. aimed at. For rapid cracking, however, the oil is retained for a longer period in the reaction chamber. For hydrating purposes, the pressure must be as high as possible, the Work being carried on with an excess of steam as compared with the oil.
The water soluble substances contained in the materials and carried away with the condensate, are removed from the latter before its re-introduction into the steam generator 2. This can be eifected in a vessel l4 in known manner, for instance by lixiviation with suitable known reagents capable of dissolving the phenols and oxides or by a fractional cooling in which the oil is automatically disengaged. This treatment of the Favourable combinations of reaction chamber I by throttling the steam at I2, in which case a pump 13 must be used for feeding the oil from the vessel 3 into the chamber l, or part of the cold water under pressure may, for condensing the steam in the vessel 3, be
passed through the latter at Hi. It is not necessaryto carry out the process in two vessels in succession, since the heat interchange and condensation of the steam under pressure can be effected in a single vessel.
The above described process can be employed in all cases when the materials are to be subjected to high pressure and to temperatures between 250 C. and 600 C. Coal paste may be treated together with hydrogen containing materials for liquefaction, and hydrocarbons and tar oils may be refined in this manner. Various hydration processes can be carried out in this manner, in which case the steamis used not only as a heating medium butalso as a reagent in known manner.
The employment of the highly superheated steam according to the present invention, does not exclude thesimultaneous use of difi'erent, chemically acting gases and vapours such as air, oxygen, hydrogen, carbon oxide, ammonia, sulphur dioxide and the like which may be introduced together with the steam through a pipe I 5.
The time of reaction is determined, as is usual in the art, by the nature of the raw material under treatment.
The process according to the invention has many technical advantages. By the employment of superheated steam a large yield of heat can be obtained from camparatively small apparatus, and the saving of heat by carrying out the process according to the present invention is considerable.
I claim:
1. A process of cracking mineral tar oils and similar substances, comprising feeding the initial substance through a dephlegmating zone into a reaction zone, generating steam at a pressure of about 200 atmospheres, feeding said steam at such pressure and at a temperature of about 500 C. through the reaction zone into the dephlegmating zone, condensing the major portion of the steam in .the dephlegmating zone into water under pressure, and utilizing said water under pressure in the steam generation.
2. The process claimed in claim 1 including the step of feeding chemically reacting gases together with thesteam into the reaction zone.
3. The process claimed in claim 1 including thestep of separating from the condensate substances dissolved in the latter during the cracking process. v
GEORG ZOTOS.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE2001444X | 1930-03-03 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2001444A true US2001444A (en) | 1935-05-14 |
Family
ID=7945459
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US548427A Expired - Lifetime US2001444A (en) | 1930-03-03 | 1931-07-02 | Process of refining oils and the like by steam treatment |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2001444A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2951805A (en) * | 1957-06-03 | 1960-09-06 | Houdry Process Corp | Cracking in the presence of a volatile acid |
| US3666828A (en) * | 1970-09-14 | 1972-05-30 | Phillips Petroleum Co | Condensate purification and recovery for use as dilution steam to pyrolysis furnace |
| US4469587A (en) * | 1983-09-02 | 1984-09-04 | Intevep, S.A. | Process for the conversion of asphaltenes and resins in the presence of steam, ammonia and hydrogen |
-
1931
- 1931-07-02 US US548427A patent/US2001444A/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2951805A (en) * | 1957-06-03 | 1960-09-06 | Houdry Process Corp | Cracking in the presence of a volatile acid |
| US3666828A (en) * | 1970-09-14 | 1972-05-30 | Phillips Petroleum Co | Condensate purification and recovery for use as dilution steam to pyrolysis furnace |
| US4469587A (en) * | 1983-09-02 | 1984-09-04 | Intevep, S.A. | Process for the conversion of asphaltenes and resins in the presence of steam, ammonia and hydrogen |
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