US4469587A
Expired / Lapsed
US
⏱️ 0.0 years remaining
Process for the conversion of asphaltenes and resins in the presence of steam, ammonia and hydrogen
Assignee: Petróleos de Venezuela SA
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Filing: 1983-09-02
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Granted: 1984-09-04
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Expires: 2003-09-02
Abstract
Abstract A process for upgrading heavy crude comprises the hydroconversion of asphaltenes and resins in the presence of steam and ammonia at high temperatures, followed by deasphalting to eliminate metals and remaining asphaltenes. By way of the process of the present invention, conversion of asphaltenes and resins is accomplished while at the same time insuring a low formation of gases and coke so as to obtain an end product with a high yield of distillates and low metal content. The process is particularly suitable for any type of heavy crude, for example those of the Orinoco zone, which possess a high content of asphaltenes and metals.
Inventors
- 👤 Roberto E. Galiasso Tailleur
- 👤 Jose A. Salazar Guillen
- 👤 Donald Huskey
- 👤 Alfredo L. Morales
- 👤 Luig G. Aquino
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-10-30 20:04
CPC Classifications
C; C10; C10G; C10G65/00; C10G65/02; C10G65/04; C10G2300/00; C10G2300/10; C10G2300/107
Claims Analysis
Total Claims: 27
Claim 1
Independent Claim
192 words
A process for upgrading heavy crude feedstock containing more than 5% asphaltenes by the controlled conversion of asphaltenes and resins comprising: (a) feeding a hydrocarbon feedstock to a first hydroconversion thermal stage wherein said hydrocarbon feedstock is treated with steam and ammonia and hydrogen so as to diminish the content of asphaltenes and resins, wherein the concentration of ammonia is about between 0.1 and 10% by volume and the ratio of the mixture of steam and ammonia is about between 0.1 and 30% by volume with respect to the hydrocarbon feedstock and wherein the ratio of hydrogen to the hydrocarbon feedstock is between about 300 and 4500 Nm 3 /m 3 ; (b) feeding the effluent from said first hydroconversion thermal stage to a second hydroconversion thermal stage wherein said effluent is further treated in the presence of steam and ammonia so as to further diminish the content of asphaltenes and resins; and (c) withdrawing the treated effluent from said second hydroconversion thermal stage and passing said treated effluent to a high pressure-high temperature separator wherein said treated effluent is separated so as to produce a liquid fraction and a residual fraction.
Claim 2
Dependent Claim
192 words
A process for upgrading heavy crude feedstock containing more than 5% asphaltenes by the controlled conversion of asphaltenes and resins comprising: (a) feeding a hydrocarbon feedstock to a first hydroconversion thermal stage wherein said hydrocarbon feedstock is treated with steam and ammonia and hydrogen so as to diminish the content of asphaltenes and resins, wherein the concentration of ammonia is about between 0.1 and 10% by volume and the ratio of the mixture of steam and ammonia is about between 0.1 and 30% by volume with respect to the hydrocarbon feedstock and wherein the ratio of hydrogen to the hydrocarbon feedstock is between about 300 and 4500 Nm 3 /m 3 ; (b) feeding the effluent from said first hydroconversion thermal stage to a second hydroconversion thermal stage wherein said effluent is further treated in the presence of steam and ammonia so as to further diminish the content of asphaltenes and resins; and (c) withdrawing the treated effluent from said second hydroconversion thermal stage and passing said treated effluent to a high pressure-high temperature separator wherein said treated effluent is separated so as to produce a liquid fraction and a residual fraction.
Claim 3
Dependent Claim
46 words
A process according to claim 1 including the steps of passing said liquid fraction to a low temperature-high pressure separator wherein hydrogen, H 2 S and NH 3 are recovered as heads, water and ammonia are removed as bottom products and a light hydrocarbon is produced.
Claim 4
Dependent Claim
37 words
A process according to claim 2 including the steps of feeding said light hydrocarbon to a low temperature-low pressure separator wherein C 1 -C 4 are recovered as heads and the condensed hydrocarbons leave as bottom products.
Claim 5
Dependent Claim
26 words
A process according to claim 1 including the steps of feeding said residual fraction to an atmospheric distillation column wherein an atmospheric pressure residue is produced.
Claim 6
Dependent Claim
27 words
A process according to claim 4 including the steps of feeding the atmospheric pressure residue to a vacuum distillation column so as to produce a vacuum residue.
Claim 7
Dependent Claim
38 words
A process according to claim 5 including the steps of feeding said vacuum residue to a decanter wherein said vacuum residue is deasphalted in the presence of water and a solvent so as to produce a deasphalted stream.
Claim 8
Dependent Claim
27 words
A process according to claim 6 including the steps of passing said deasphalted stream to an evaporator so as to evaporate the solvent from said deasphalted stream.
Claim 9
Dependent Claim
41 words
A process according to claim 7 including the steps of passing said deasphalted stream from said evaporator to a water recovery unit and thereafter feeding said deasphalted stream to a hydrotreatment unit wherein sulfur and vanadium are eliminated from said stream.
Claim 10
Dependent Claim
58 words
A process according to claim 1 wherein a mixture of steam and ammonia is introduced into said first hydroconversion thermal stage wherein the concentration of ammonia is about between 0.3 and 8% by volume and the ratio of the mixture of steam and ammonia is about between 0.5 and 10% by volume with respect to the hydrocarbon feedstock.
Claim 11
Dependent Claim
17 words
A process according to claim 1 further including feeding preheated hydrogen to said first hydroconversion thermal stage.
Claim 12
Dependent Claim
23 words
A process according to claim 1 wherein the residence time in said first hydroconversion thermal stage is between about 0.32 and 64.3 minutes.
Claim 13
Dependent Claim
31 words
A process according to claim 1 wherein the temperature of the liquid in the first thermal stage is progressively increased up to a maximum of about between 420° and 540° C.
Claim 14
Dependent Claim
31 words
A process according to claim 1 wherein the temperature of the liquid in the first thermal stage is progressively increased up to a maximum of about between 440° and 500° C.
Claim 15
Dependent Claim
23 words
A process according to claim 1 wherein the operating pressure in said first hydroconversion thermal stage is about between 20 and 200 atmospheres.
Claim 16
Dependent Claim
23 words
A process according to claim 1 wherein the operating pressure in said first hydroconversion thermal stage is about between 50 and 150 atmospheres.
Claim 17
Dependent Claim
20 words
A process according to claim 1 including the steps of providing a helicoidal reactor for said first hydroconversion thermal stage.
Claim 18
Dependent Claim
24 words
A process according to claim 6 wherein the percentage of water with respect to the solvent is about between 5 and 20% by volume.
Claim 19
Dependent Claim
21 words
A process according to claim 17 wherein the solvent is a hydrocarbon comprising C 5 to C 7 or mixtures thereof.
Claim 20
Dependent Claim
33 words
A process according to claim 6 wherein the deasphalting is carried out at a temperature of about between 180° and 230° C. and at a pressure of about between 15 and 50 atmospheres.
Claim 21
Dependent Claim
19 words
A process according to claim 6 wherein the solvent/vacuum residue ratio is about between 2:1 and 10:1 by volume.
Claim 22
Dependent Claim
19 words
A process according to claim 6 wherein the solvent/vacuum residue ratio is about between 4:1 and 9:1 by volume.
Claim 23
Dependent Claim
64 words
A process according to claim 1 including the steps of providing a bubble column type reactor for said second thermal hydroconversion stage wherein the bubble column type reactor is provided with distributors so as to form gas bubbles having a diameter of no greater than 10 cm and wherein the coefficient of axial dispersion is about between 40 and 200 cm 2 per second.
Claim 24
Dependent Claim
69 words
A process according to claim 8 including the steps of providing a fixed bed reactor as the hydrotreatment unit and providing a porous catalyst in said fixed bed reactor wherein more than 40% of the pores have a radius of greater than 100 Å, a surface area of about between 150 and 300 m 2 /g and a pore volume of about between 0.8 and 1.2 cm 3 /g.
Claim 25
Dependent Claim
30 words
A process according to claim 8 wherein the hydrotreatment takes place at pressures of about between 20 and 200 atmospheres and a temperature of about between 350° and 440° C.
Claim 26
Dependent Claim
30 words
A process according to claim 8 wherein the hydrotreatment takes place at pressures of about between 50 and 150 atmospheres and a temperature of about between 370° and 430° C.
Claim 27
Dependent Claim
20 words
A process according to claim 24 wherein the hydrogen/hydrocarbon ratio varies between 100 and 2,000 Nm 3 /m 3 .
References Cited (Backward Citations)
US2001444A
Cited
US2413407A
Cited
US2704738A
Cited
US2847353A
Cited
US3136712A
Cited
US3321394A
Cited
US3353920A
Cited
US3557241A
Cited
US3562146A
Cited
US3622499A
Cited
US3666658A
Cited
US3761538A
Cited
US3794580A
Cited
US3848017A
Cited
US4214979A
Cited
US4191636A
Cited
US4159937A
Cited
US4400264A
Cited
USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1987-09-04 | 1988-03-05 | 1988-09-04 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1991-09-04 | 1992-03-05 | 1992-09-04 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1995-09-04 | 1996-03-05 | 1996-09-04 | $7700.00 | Window Closed / Lapsed |