USRE39244E1 - Acid gas disposal - Google Patents
Acid gas disposal Download PDFInfo
- Publication number
- USRE39244E1 USRE39244E1 US10/937,789 US93778904A USRE39244E US RE39244 E1 USRE39244 E1 US RE39244E1 US 93778904 A US93778904 A US 93778904A US RE39244 E USRE39244 E US RE39244E
- Authority
- US
- United States
- Prior art keywords
- acid gas
- water
- pressure
- gas
- dense fluid
- 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
Images
Classifications
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B41/00—Equipment or details not covered by groups E21B15/00 - E21B40/00
- E21B41/005—Waste disposal systems
- E21B41/0057—Disposal of a fluid by injection into a subterranean formation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE
- B09B1/00—Dumping solid waste
Definitions
- Acid gas as used herein is defined as a gaseous mixture of varying concentrations of carbon dioxide (CO 2 ) and hydrogen sulfide (H 2 S) resulting from treating processes employed to remove these contaminants from sour hydrocarbon streams such as produced natural gas. These mixtures often are water saturated and contain small amounts of hydrocarbons, treating solvents, absorbants, and other matter.
- CO 2 carbon dioxide
- H 2 S hydrogen sulfide
- BEARD in U.S. Pat. No. 5,340,382 disclosed the process of absorbing acid gas at about 400 psi into produced water by a static mixing unit and then pumping the solution into a disposal well.
- the BEARD process uses about 160 barrels water for about 1,000 cu. ft. of acid gas. If the acid gas were liquified, this would be a ratio (by volume) of approximately 424 H 2 O:1 dense fluid acid gas.
- Sulfur recovery plants are another method of dealing with acid gas. This process utilizes catalyst beds to convert over 99% of the H 2 S to elemental sulfur. The process off gas is incinerated resulting in release of associated carbon and sulfur dioxides as emissions to the atmosphere.
- This invention disposes of the acid gases by forming the acid gas into a dense aqueous fluid by compression followed by cooling. Then the dense fluid is mixed at high pressure (circa 650 to 2,000 psi) with water.
- the acid gas as a dense fluid may be referred to as liquified gas or aqueous gas.
- the term “liquified” or “aqueous” is used in this application to include dense compressed gases which might not technically be a liquid.
- the alkaline water may be referred to as brackish water or salt water disposal (SWD) water. Although alkaline water is preferred, water with pH below 7.0 may be used as necessary.
- a pressure regulated valve controls the pressure of the liquified gas and the water to a suitable pressure until they are mixed. Thereafter the pressure regulated valve releases the mixture into a disposal well.
- An object of this invention is to dispose of acid gas.
- Another object of this invention is to dispose of the acid gas along with the disposing of unwanted alkaline water and other undesirable liquids.
- the drawing is a flow diagram of the process involved.
- a source 10 of acid gas resulting from a source such as the treating system for a sour natural gas stream.
- a source of alkaline water 12 resulting from the production of petroleum products is available.
- the source 12 alkaline water might be a well drilled to a strata producing alkaline water. Although fresh water is operable, greater alkalinity, found in brackish water, results in more neutral solution.
- the acid gas from the source 10 is compressed by compressor 14 . After the gas is compressed it is cooled by cooler 16 .
- compressor 14 and cooler 16 are each shown as single elements, the compression will normally be in stages with cooling after each stage. Also, those skilled in the art are familiar with compressors, coolers, etc. to compress acid gas to pressures necessary for operation, i.e. approximately 650 to 2000 psi.
- Cooler 16 sufficiently cools the acid gas until it condenses to a dense fluid.
- the water is pumped by pump 18 to a high pressure.
- Tee connection 20 receives the mixture from Tee 20 .
- Check valve 22 between the acid gas cooler 16 and the Tee 20 prevents the flow of water from the pump 18 into the cooler 16 .
- check valve 24 prevents flow of acid gas dense fluid toward the pump 18 .
- Confluent pressure gage 36 indicates the pressure in the confluent line 25 . There is no minimum length for the confluent line 25 except for physical structural limitations.
- Pressure valve 26 controls the pressure in confluent line 25 at a suitably high pressure to prevent vaporization of the acid gas dense fluid.
- the pressure control valve will control the pressure at the Tee connection to a range of approximately 650-2000 psi. With a high percentage (e.g. 83%) of H 2 S the pressure may be as low as 650 psi and with a high percentage of CO 2 (e.g. 75%) the pressure may be as high as 1900 psi. The increase in minimum pressure also will approximate a linear relationship to the percentage of CO 2 .
- the pressure control valve 26 discharges the mixture into an injection tube 32 which extends into the disposal well 28 .
- the injection tube 32 normally has a well head assembly (not shown in drawings) to control the flow.
- the well head assembly could include both manual and automatic valves.
- the mixture of acid gas dense fluid and water is injected into the disposal well into a suitable strata 30 deep within the earth.
- the size of the compressor will be determined by the amount of acid gas requiring disposal. This amount will generally be known at the time the equipment is assembled. The cooler likewise will be sufficient to cool the compressed gases to a liquid or dense fluid state. The minimum water requirements will depend upon the amount of acid gas to be disposed and also the composition of the acid gas.
- hydrogen sulfide is more soluble in water than carbon dioxide.
- the gas for disposal is about 83% hydrogen sulfide and 17% carbon dioxide the disposal process will require approximately two units of water for one unit of aqueous acid gas.
- the percentages of hydrogen sulfide and carbon dioxide are by mole percent.
- the unit of water and acid gas dense fluid is by volume.
- aqueous acid gas has about 50% hydrogen sulfide and about 50% carbon dioxide, a 5:1 ratio of water to dense fluid is satisfactory.
- the aqueous mixture is about 25% hydrogen sulfide and about 75% carbon dioxide to 8:1 water to dense fluid ratio is required. Basically and approximately the minimum volume of water for one volume of acid gas dense fluid will be a linear relationship.
- the upper temperature limit of acid gas dense fluid at check valve 22 and the mix in the confluent line 25 is approximately 140° F.
- the preferred temperature of the acid gas at the check valve 22 is below 130° F., and of the mix in the confluent line 25 is below 110° F.
- the lower operation limit of temperatures is freezing of the fluid involved.
- the above ratios of water to acid gas dense fluid are approximately the minimal amount of water required. If lesser water is used, difficulties may be experienced. If there is an excess of alkaline water to be disposed of in excess of the minimum requirements there is no problem in mixing the additional water into the Tee 20 . Those with ordinary skill will know how to proportion the desired volume of water to the volume of acid gas dense fluid. If other compatible and suitable liquids require disposal, they too may be pumped into the confluent line 25 .
- the pressures are also approximately the minimal pressures to form a dense fluid at temperatures below 120° F. at the check valve 22 .
- the maximum pressures are limited only by the higher cost of higher pressures.
- injection pressure it is meant that pressure at the well head, which is at the top of the disposal well 28 .
- Injection pressure gage 34 in the injection tube 32 down stream from the control valve 26 indicates the injection pressure.
- the pressure in the injection tube at the pressure gage 34 will be responsive to different events. Obviously the pressure gage 34 will increase with an increased volume of liquids being pumped. For example, if pump 18 were to pump twice as much water, the hydraulic flow in the injection tube would result in a higher pressure at pressure gage 34 . Also, as the disposal well is operated, different solids, for example, chemical precipitates or the like will begin to collect in the strata 30 which will reduce its porosity surrounding the disposal well 28 . This build-up is to be expected and will result in a slow increase in injection pressure. Such an increase in pressure might normally be no more than 1 psi per day.
- hydrates will form and adhere to the well surfaces, particularly the inside bore of the injection tube 32 . If hydrates form they would be an indication that there was insufficient water being mixed with the aqueous acid gas. This would result in a pressure increase in the range of 5 or 10 pounds per square inch per hour until no flow could be achieved.
- the preferred operation includes that manual process calculations or a computer process simulation be conducted with a complete analysis of the acid gas and water to be used. When this simulation is completed, the appropriate process pressures and temperatures can be determined for optimum performance.
- Such computer simulations can be made with HYSYS software available from Hyprotech, Inc., located in Houston, Tex. for example.
- the operator can adjust the ratio of water to acid gas dense fluid to obtain stable and satisfactory operating conditions. Normally the unstable conditions will result from an insufficient amount of water for the amount of aqueous acid gas being injected.
- the confluent line 25 be of a material which resists corrosion from the acid gas and alkaline water mixture.
- suitable grades of stainless steel for this purpose are well known in the art and in certain cases it is necessary to solution treat and/or coat the stainless steel before it is put into service. Those skilled in the art will know of the materials of construction for the confluent line.
Abstract
Acid gas is liquified by compression and cooling, mixed with water under pressure and flowed into a disposal well.
Description
This application is a divisional application of Reissue application Ser. No. 10/300,265, filed Nov. 20, 2002, which is a reissue of U.S. Pat. No. 6,149,344, filed Nov. 21, 2000, which claims priority to provisional application Ser. No. 60/061,042, filed Oct. 4, 1997.
Applicant filed a Provisional Application on this subject matter on Oct. 4, 1997, Serial No. 60/061,043. Specific reference is made to that document.
(1) Field of the Invention
This invention relates to disposal of acid gases. Acid gas as used herein is defined as a gaseous mixture of varying concentrations of carbon dioxide (CO2) and hydrogen sulfide (H2S) resulting from treating processes employed to remove these contaminants from sour hydrocarbon streams such as produced natural gas. These mixtures often are water saturated and contain small amounts of hydrocarbons, treating solvents, absorbants, and other matter.
(2) Description of the Related Art
Before this invention, BEARD in U.S. Pat. No. 5,340,382 disclosed the process of absorbing acid gas at about 400 psi into produced water by a static mixing unit and then pumping the solution into a disposal well. The BEARD process uses about 160 barrels water for about 1,000 cu. ft. of acid gas. If the acid gas were liquified, this would be a ratio (by volume) of approximately 424 H2O:1 dense fluid acid gas.
In Canada (where the acid gases have high hydrogen sulfide content) acid gas is dehydrated, compressed, and injected into disposal wells. Reports of such are found in the Oil & Gas Journal of Apr. 18, 1997 by Edward Wichert and Tom Royan; the 1996 paper given by H. L. Longworth, G. C. Dunn and M. Semchuck at the gas and technology conference held in Calgary, Alberta from the 28th of April until May 1, 1996; the paper of Wichert and Royan given at the same meeting in 1996.
Sulfur recovery plants are another method of dealing with acid gas. This process utilizes catalyst beds to convert over 99% of the H2S to elemental sulfur. The process off gas is incinerated resulting in release of associated carbon and sulfur dioxides as emissions to the atmosphere.
This invention disposes of the acid gases by forming the acid gas into a dense aqueous fluid by compression followed by cooling. Then the dense fluid is mixed at high pressure (circa 650 to 2,000 psi) with water.
Occasionally herein the forming of the acid gas into a dense fluid will be referred to as liquefying, and the acid gas as a dense fluid may be referred to as liquified gas or aqueous gas. The term “liquified” or “aqueous” is used in this application to include dense compressed gases which might not technically be a liquid. Also, the alkaline water may be referred to as brackish water or salt water disposal (SWD) water. Although alkaline water is preferred, water with pH below 7.0 may be used as necessary.
A pressure regulated valve controls the pressure of the liquified gas and the water to a suitable pressure until they are mixed. Thereafter the pressure regulated valve releases the mixture into a disposal well.
An object of this invention is to dispose of acid gas.
Another object of this invention is to dispose of the acid gas along with the disposing of unwanted alkaline water and other undesirable liquids.
Further objects are to achieve the above with equipment that is sturdy, compact, durable, simple, safe, efficient, versatile, ecologically compatible, energy conserving, and reliable, yet inexpensive and easy to manufacture, install, operate, and maintain.
Other objects are to achieve the above with a method that is rapid, versatile, ecologically compatible, energy conserving, efficient, and inexpensive, and does not require highly skilled people to install, operate, and maintain.
The specific nature of the invention, as well as other objects, uses, and advantages thereof, will clearly appear from the following description and from the accompanying drawings.
The drawing is a flow diagram of the process involved.
As an aid to correlating the terms to the exemplary drawings(s), the following catalog of elements is provided:
- 10 source of acid gas
- 12 source of water
- 14 compressor
- 16 cooler
- 18 pump
- 20 Tee connection
- 22 check valve
- 24 check valve
- 25 confluent line
- 26 pressure control valve
- 28 disposal well
- 30 strata
- 32 injection tube
- 34 injection pressure gage
- 36 confluent pressure gage
According to this invention there will be a source 10 of acid gas resulting from a source such as the treating system for a sour natural gas stream. Usually a source of alkaline water 12 resulting from the production of petroleum products is available. In the event that there is insufficient alkaline water to be disposed of, the source 12 alkaline water might be a well drilled to a strata producing alkaline water. Although fresh water is operable, greater alkalinity, found in brackish water, results in more neutral solution.
The acid gas from the source 10 is compressed by compressor 14. After the gas is compressed it is cooled by cooler 16. Those skilled in the art will understand that although the compressor 14 and cooler 16 are each shown as single elements, the compression will normally be in stages with cooling after each stage. Also, those skilled in the art are familiar with compressors, coolers, etc. to compress acid gas to pressures necessary for operation, i.e. approximately 650 to 2000 psi.
It is important not to produce bulk aqueous acid gas before the final compression stage. Cooler 16 sufficiently cools the acid gas until it condenses to a dense fluid.
The water is pumped by pump 18 to a high pressure.
The acid gas dense fluid and the high pressure water are combined by Tee connection 20. Although the connection 20 is described as a Tee, it will be understood that the connection of the two flows could be in the form of a Y or a 45° connection. Confluent line 25 receives the mixture from Tee 20. Check valve 22 between the acid gas cooler 16 and the Tee 20 prevents the flow of water from the pump 18 into the cooler 16. Likewise check valve 24 prevents flow of acid gas dense fluid toward the pump 18. Confluent pressure gage 36 indicates the pressure in the confluent line 25. There is no minimum length for the confluent line 25 except for physical structural limitations.
The pressure control valve 26 discharges the mixture into an injection tube 32 which extends into the disposal well 28. The injection tube 32 normally has a well head assembly (not shown in drawings) to control the flow. The well head assembly could include both manual and automatic valves. The mixture of acid gas dense fluid and water is injected into the disposal well into a suitable strata 30 deep within the earth.
The size of the compressor will be determined by the amount of acid gas requiring disposal. This amount will generally be known at the time the equipment is assembled. The cooler likewise will be sufficient to cool the compressed gases to a liquid or dense fluid state. The minimum water requirements will depend upon the amount of acid gas to be disposed and also the composition of the acid gas.
Basically hydrogen sulfide is more soluble in water than carbon dioxide. As one example, if the gas for disposal is about 83% hydrogen sulfide and 17% carbon dioxide the disposal process will require approximately two units of water for one unit of aqueous acid gas. The percentages of hydrogen sulfide and carbon dioxide are by mole percent. The unit of water and acid gas dense fluid is by volume.
As another example, if aqueous acid gas has about 50% hydrogen sulfide and about 50% carbon dioxide, a 5:1 ratio of water to dense fluid is satisfactory.
As another example, if the aqueous mixture is about 25% hydrogen sulfide and about 75% carbon dioxide to 8:1 water to dense fluid ratio is required. Basically and approximately the minimum volume of water for one volume of acid gas dense fluid will be a linear relationship.
The minimum water and pressure for the normal range of operation may be estimated as follows:
RH2 O=0.25−0.10345×CO2%
Pmin=284+21.55×CO2%
Where
RH
Pmin=284+21.55×CO2%
Where
-
- RH
2 O is the minimum ratio by volume of water having at least a pH of 7.5 to the dense fluid acid gas. (i.e. RH2 O:1AG where AG is unit volume of acid gas). - Pmin is the minimum pressure in the confluent line in psi.
- CO2% is the percent of CO2 in a mixture of acid gas on a mole basis.
- RH
The above formulas are for temperatures in the range of 60° to 140° F. in the confluent line 25.
The upper temperature limit of acid gas dense fluid at check valve 22 and the mix in the confluent line 25 is approximately 140° F. The preferred temperature of the acid gas at the check valve 22 is below 130° F., and of the mix in the confluent line 25 is below 110° F.
The lower operation limit of temperatures is freezing of the fluid involved.
The above ratios of water to acid gas dense fluid are approximately the minimal amount of water required. If lesser water is used, difficulties may be experienced. If there is an excess of alkaline water to be disposed of in excess of the minimum requirements there is no problem in mixing the additional water into the Tee 20. Those with ordinary skill will know how to proportion the desired volume of water to the volume of acid gas dense fluid. If other compatible and suitable liquids require disposal, they too may be pumped into the confluent line 25.
The pressures are also approximately the minimal pressures to form a dense fluid at temperatures below 120° F. at the check valve 22. The maximum pressures are limited only by the higher cost of higher pressures.
There must be sufficient water to form a stable mixture at the injection pressure. By injection pressure it is meant that pressure at the well head, which is at the top of the disposal well 28. Injection pressure gage 34 in the injection tube 32 down stream from the control valve 26 indicates the injection pressure.
If less than 5% of the mixture of alkaline water and aqueous acid gas vaporizes at this point, normally satisfactory operation will be maintained. If no greater amount of gas than 5% is formed within the flow of the mixture; the gas will normally be in the form of small bubbles. These bubbles will be carried by the flow of fluid into the disposal well 28. As the mixture descends into the disposal well 28 there will be a pressure increase which will force the vapor back into a liquid or dense fluid phase.
If there is insufficient water to form a stable mixture such that more than 5% gas vaporizes; a gas pocket will often form within the injection tube 32 at about the top of the disposal well. This gas pocket will cause an increase in pressure and the operation will become unstable at that time.
The pressure in the injection tube at the pressure gage 34 will be responsive to different events. Obviously the pressure gage 34 will increase with an increased volume of liquids being pumped. For example, if pump 18 were to pump twice as much water, the hydraulic flow in the injection tube would result in a higher pressure at pressure gage 34. Also, as the disposal well is operated, different solids, for example, chemical precipitates or the like will begin to collect in the strata 30 which will reduce its porosity surrounding the disposal well 28. This build-up is to be expected and will result in a slow increase in injection pressure. Such an increase in pressure might normally be no more than 1 psi per day.
Also, under certain condition hydrates will form and adhere to the well surfaces, particularly the inside bore of the injection tube 32. If hydrates form they would be an indication that there was insufficient water being mixed with the aqueous acid gas. This would result in a pressure increase in the range of 5 or 10 pounds per square inch per hour until no flow could be achieved.
The preferred operation includes that manual process calculations or a computer process simulation be conducted with a complete analysis of the acid gas and water to be used. When this simulation is completed, the appropriate process pressures and temperatures can be determined for optimum performance. Such computer simulations can be made with HYSYS software available from Hyprotech, Inc., located in Houston, Tex. for example.
With these different operating criteria the operator can adjust the ratio of water to acid gas dense fluid to obtain stable and satisfactory operating conditions. Normally the unstable conditions will result from an insufficient amount of water for the amount of aqueous acid gas being injected.
From the above it may be seen that it is desirable to always have water flowing into the disposal well even if there is no acid gas being liquified and disposed of at the time.
It is desirable that the confluent line 25 be of a material which resists corrosion from the acid gas and alkaline water mixture. The suitable grades of stainless steel for this purpose are well known in the art and in certain cases it is necessary to solution treat and/or coat the stainless steel before it is put into service. Those skilled in the art will know of the materials of construction for the confluent line.
The embodiment shown and described above is only exemplary. I do not claim to have invented all the parts, elements or steps described. Various modifications can be made in the construction, material, arrangement, and operation, and still be within the scope of my invention.
The restrictive description and drawings of the specific examples above do not point out what an infringement of this patent would be, but are to enable one skilled in the art to make and use the invention. The limits of the invention and the bounds of the patent protection are measured by and defined in the following claims.
Claims (21)
1. The method of disposing acid gas removed from hydrocarbon products comprising the steps of:
a) compressing the acid gas to a pressure wherein the acid gas will form a dense fluid,
b) forming a dense fluid by cooling the compressed acid gas,
c) mixing the acid gas as a dense fluid with sufficient water to form a stable mixture at injection pressure, and
d) injecting said stable mixture at injection pressure into a disposal well.
2. The method as defined in claim 1 wherein said compression pressure is at least 650 psi.
3. The method as defined in claim 1 wherein said water is alkaline and has a pH of at least 7.5.
4. The method as defined in claim 1 wherein a minimum pressure of step a) is Pmin=284+21.55×CO2% wherein Pmin is said minimum pressure in psi and CO2% is the percentage of carbon dioxide in the acid gas.
5. The method as defined in claim 4 wherein the compressed acid gas is cooled to a temperature of below 130° F.
6. The method as defined in claim 1 wherein insufficient water is a minimum of
RH2 O=0.25+0.10345×CO2%
RH
wherein RH 2 O is the minimum ratio by volume of water having at least a pH of 7.5 to the dense fluid acid gas.
7. The method as defined in claim 6 wherein the mixed acid gas and water has a temperature of below 110° F.
8. The method as defined in claim 1 further comprising:
e) mixing the acid gas and water in a confluent line, and
f) maintaining the pressure in the confluent line to the compression pressure by
g) limiting the flow from the confluent line by a pressure control valve.
9. The method as defined in claim 8 wherein
h) determining that the mixture found is stable by less than a significant amount of any component of the acid gas flashing into the gas phase down stream from the control valve.
10. The method as defined in claim 9 wherein determining that the amount of any component of acid gas flashed is more than a significant amount by formation of hydrates adhering on surfaces of the disposal well.
11. The method as defined in claim 9 wherein determining that the amount of any component of acid gas flashed is more than a significant amount by formation of gas pockets down stream of the control valve as determined by rapid increase of pressure down stream of the control valve.
12. The method as defined in claim 9 wherein less than a significant amount of any component of acid gas is flashed is determined when less the 5 percent of said mixture is flashed.
13. The method as defined in claim 9 wherein less than a significant amount of any component of acid gas is flashed is determined by process simulation.
14. The method as defined in claim 9 wherein less than a significant amount of any component of acid gas is flashed is determined by manual process calculations.
15. A system for disposing of acid gas comprising:
a source of acid gas;
a source of water;
a series of at least one compressor and one cooler to compress and cool the acid gas to form a dense fluid acid gas;
a gas line to convey the dense fluid acid gas from its source to a confluent line;
a water line to convey the water from its source to the confluent line;
a mixer connecting the gas and water lines to the confluent line, the mixture for mixing water and acid gas into a stable mixture; and
an injection tube for injecting the stable mixture of water and acid gas of the confluent line into a disposal well.
16. The disposal system of claim 15 further comprising a pressure controller in the confluent line.
17. The disposal system of claim 16 wherein the pressure controller maintains the pressure at a level sufficient to prevent substantial vaporization of the mixed water and acid gas.
18. The disposal system of claim 15 wherein water is continuously pumped through the injection tube to the disposal well even when no dense fluid acid gas is being disposed.
19. A method of injecting a liquid containing acid gas into a disposal well comprising the steps of:
forming the liquid by mixing water and dense fluid acid gas to form a stable mixture at a pressure; and
maintaining the pressure on the liquid prior to injection at a level sufficient to prevent substantial vaporization of the liquid.
20. The method according to claim 19 wherein the pressure is maintained at about 650 psi or higher.
21. The system according to claim 15 , wherein the mixer comprises:
a tee connection fluidly connecting the water and gas lines to the confluent line; and
a check valve in each of the water and gas lines to prevent backflow of the stable mixture into the gas and water lines.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US10/937,789 USRE39244E1 (en) | 1997-10-04 | 2004-09-09 | Acid gas disposal |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US6104397P | 1997-10-04 | 1997-10-04 | |
US09/159,986 US6149344A (en) | 1997-10-04 | 1998-09-24 | Acid gas disposal |
US10/300,265 USRE39077E1 (en) | 1997-10-04 | 2002-11-20 | Acid gas disposal |
US10/937,789 USRE39244E1 (en) | 1997-10-04 | 2004-09-09 | Acid gas disposal |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/159,986 Reissue US6149344A (en) | 1997-10-04 | 1998-09-24 | Acid gas disposal |
Publications (1)
Publication Number | Publication Date |
---|---|
USRE39244E1 true USRE39244E1 (en) | 2006-08-22 |
Family
ID=26740672
Family Applications (3)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/159,986 Ceased US6149344A (en) | 1997-10-04 | 1998-09-24 | Acid gas disposal |
US10/300,265 Expired - Lifetime USRE39077E1 (en) | 1997-10-04 | 2002-11-20 | Acid gas disposal |
US10/937,789 Expired - Lifetime USRE39244E1 (en) | 1997-10-04 | 2004-09-09 | Acid gas disposal |
Family Applications Before (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/159,986 Ceased US6149344A (en) | 1997-10-04 | 1998-09-24 | Acid gas disposal |
US10/300,265 Expired - Lifetime USRE39077E1 (en) | 1997-10-04 | 2002-11-20 | Acid gas disposal |
Country Status (1)
Country | Link |
---|---|
US (3) | US6149344A (en) |
Cited By (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7644765B2 (en) | 2006-10-20 | 2010-01-12 | Shell Oil Company | Heating tar sands formations while controlling pressure |
US7673786B2 (en) | 2006-04-21 | 2010-03-09 | Shell Oil Company | Welding shield for coupling heaters |
US7798220B2 (en) | 2007-04-20 | 2010-09-21 | Shell Oil Company | In situ heat treatment of a tar sands formation after drive process treatment |
US7866386B2 (en) | 2007-10-19 | 2011-01-11 | Shell Oil Company | In situ oxidation of subsurface formations |
US20120038174A1 (en) * | 2010-08-13 | 2012-02-16 | Board Of Regents, The University Of Texas System | Storing Carbon Dioxide and Producing Methane and Geothermal Energy from Deep Saline Aquifers |
US8151907B2 (en) | 2008-04-18 | 2012-04-10 | Shell Oil Company | Dual motor systems and non-rotating sensors for use in developing wellbores in subsurface formations |
US20120090838A1 (en) * | 2007-11-06 | 2012-04-19 | Bp Exploration Operating Company Limited | Method of injecting carbon dioxide |
US8220539B2 (en) | 2008-10-13 | 2012-07-17 | Shell Oil Company | Controlling hydrogen pressure in self-regulating nuclear reactors used to treat a subsurface formation |
US8225866B2 (en) | 2000-04-24 | 2012-07-24 | Shell Oil Company | In situ recovery from a hydrocarbon containing formation |
US8230927B2 (en) | 2005-04-22 | 2012-07-31 | Shell Oil Company | Methods and systems for producing fluid from an in situ conversion process |
US8327932B2 (en) | 2009-04-10 | 2012-12-11 | Shell Oil Company | Recovering energy from a subsurface formation |
US8608249B2 (en) | 2001-04-24 | 2013-12-17 | Shell Oil Company | In situ thermal processing of an oil shale formation |
US8627887B2 (en) | 2001-10-24 | 2014-01-14 | Shell Oil Company | In situ recovery from a hydrocarbon containing formation |
US8631866B2 (en) | 2010-04-09 | 2014-01-21 | Shell Oil Company | Leak detection in circulated fluid systems for heating subsurface formations |
US8701769B2 (en) | 2010-04-09 | 2014-04-22 | Shell Oil Company | Methods for treating hydrocarbon formations based on geology |
US8820406B2 (en) | 2010-04-09 | 2014-09-02 | Shell Oil Company | Electrodes for electrical current flow heating of subsurface formations with conductive material in wellbore |
US9016370B2 (en) | 2011-04-08 | 2015-04-28 | Shell Oil Company | Partial solution mining of hydrocarbon containing layers prior to in situ heat treatment |
US9033042B2 (en) | 2010-04-09 | 2015-05-19 | Shell Oil Company | Forming bitumen barriers in subsurface hydrocarbon formations |
US9309755B2 (en) | 2011-10-07 | 2016-04-12 | Shell Oil Company | Thermal expansion accommodation for circulated fluid systems used to heat subsurface formations |
Families Citing this family (32)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6289988B1 (en) * | 2000-03-24 | 2001-09-18 | Exxonmobil Research And Engineering Company | Process for management of industrial wastes |
GB0022688D0 (en) * | 2000-09-15 | 2000-11-01 | Ingen Process Ltd | Removal and disposal of sour reservoir components |
US6755251B2 (en) | 2001-09-07 | 2004-06-29 | Exxonmobil Upstream Research Company | Downhole gas separation method and system |
MY129091A (en) | 2001-09-07 | 2007-03-30 | Exxonmobil Upstream Res Co | Acid gas disposal method |
US6620091B1 (en) * | 2001-09-14 | 2003-09-16 | Chevron U.S.A. Inc. | Underwater scrubbing of CO2 from CO2-containing hydrocarbon resources |
US6919156B2 (en) * | 2002-09-25 | 2005-07-19 | Kao Corporation | Toner |
CA2414949C (en) | 2002-12-20 | 2010-04-13 | Imperial Oil Resources Limited | Integrated water treatment and flue gas desulfurization process |
WO2006115965A2 (en) * | 2005-04-21 | 2006-11-02 | Shell Internationale Research Maatschappij B.V. | Systems and methods for producing oil and/or gas |
US20070072712A1 (en) * | 2005-09-26 | 2007-03-29 | Chernick Mark J | Supple core sports ball and its associated method of manufacture |
RU2415256C2 (en) * | 2006-04-27 | 2011-03-27 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | System and procedure for extraction of oil and/or gas |
WO2007131976A1 (en) * | 2006-05-16 | 2007-11-22 | Shell Internationale Research Maatschappij B.V. | A process for the manufacture of carbon disulphide |
EP2021278A1 (en) * | 2006-05-16 | 2009-02-11 | Shell Internationale Research Maatschappij B.V. | A process for the manufacture of carbon disulphide |
US8136590B2 (en) * | 2006-05-22 | 2012-03-20 | Shell Oil Company | Systems and methods for producing oil and/or gas |
JP5347154B2 (en) * | 2006-06-28 | 2013-11-20 | 小出 仁 | CO2 underground storage processing method and system |
EA012887B1 (en) | 2006-07-07 | 2009-12-30 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Process for the manufacture of carbon disulphide |
AU2007286270A1 (en) | 2006-08-10 | 2008-02-21 | Shell Internationale Research Maatschappij B.V. | Methods for producing oil and/or gas |
US8366349B2 (en) * | 2006-11-13 | 2013-02-05 | Beachner Construction Company, Inc. | System and method for aggregate disposal |
CN101595198B (en) * | 2007-02-16 | 2013-05-08 | 国际壳牌研究有限公司 | Systems and methods for absorbing gases into a liquid |
CA2693942C (en) * | 2007-07-19 | 2016-02-02 | Shell Internationale Research Maatschappij B.V. | Methods for producing oil and/or gas |
CN101842549B (en) * | 2007-10-31 | 2013-11-20 | 国际壳牌研究有限公司 | Systems and methods for producing oil and/or gas |
CA2706083A1 (en) * | 2007-11-19 | 2009-05-28 | Shell Internationale Research Maatschappij B.V. | Systems and methods for producing oil and/or gas |
CA2705199A1 (en) | 2007-11-19 | 2009-05-28 | Shell Internationale Research Maatschappij B.V. | Producing oil and/or gas with emulsion comprising miscible solvent |
CN101959992B (en) * | 2008-02-27 | 2013-09-04 | 国际壳牌研究有限公司 | Systems and methods for producing oil and/or gas |
RU2525406C2 (en) * | 2008-04-16 | 2014-08-10 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | System and method of oil and/or gas production |
RU2494239C2 (en) * | 2008-04-16 | 2013-09-27 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | Oil and/or gas extraction system and method |
US8783371B2 (en) * | 2009-01-08 | 2014-07-22 | Gerald Blount | Subsurface capture of carbon dioxide |
US8523487B2 (en) * | 2009-06-25 | 2013-09-03 | International Business Machines Corporation | Co-disposal and co-storage of desalination concentrated brine waste product and carbon dioxide waste product |
AU2011372318B2 (en) * | 2011-06-30 | 2017-01-12 | Statoil Petroleum As | A method for storing carbon dioxide compositions in subterranean geological formations and an arrangement for use in such methods |
UA110553C2 (en) * | 2011-12-15 | 2016-01-12 | Лінк Енерджі Лтд | A pressurized alkali dispersion supply system for use in permeabilizing a coal seam |
RU2520121C2 (en) * | 2012-07-20 | 2014-06-20 | Общество С Ограниченной Ответственностью Научно-Исследовательский И Проектный Институт По Обустройству Нефтяных И Газовых Месторождений | Method of acid gas treatment for injection into formation through injector |
CN108487884A (en) * | 2018-03-19 | 2018-09-04 | 中国石油大学(华东) | A kind of deep profile correction combination individual well water injection rate adjustment improves the technical method of recovery ratio |
US11624264B2 (en) * | 2020-10-15 | 2023-04-11 | Saudi Arabian Oil Company | Controlling corrosion within wellbores |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3360945A (en) * | 1965-02-25 | 1968-01-02 | Lummus Co | Repressurized natural gas addition to main gas stream to maintain well head pressure |
US4044831A (en) * | 1975-04-02 | 1977-08-30 | Texaco Inc. | Secondary recovery process utilizing water saturated with gas |
US4169133A (en) * | 1977-02-08 | 1979-09-25 | Krupp-Koppers Gmbh | Process for recovering acidic gases collected during gas desulfurization |
US4285917A (en) * | 1980-07-31 | 1981-08-25 | Bayside Holding Corp. | Method for removal of hydrogen sulfide from sour gas streams |
US4449994A (en) * | 1982-01-15 | 1984-05-22 | Air Products And Chemicals, Inc. | Low energy process for separating carbon dioxide and acid gases from a carbonaceous off-gas |
US4576615A (en) * | 1984-08-20 | 1986-03-18 | The Randall Corporation | Carbon dioxide hydrocarbons separation process |
US4848467A (en) * | 1988-02-16 | 1989-07-18 | Conoco Inc. | Formation fracturing process |
US5340382A (en) * | 1993-07-08 | 1994-08-23 | Beard Thomas L | Acid gas absorption process |
US5344627A (en) * | 1992-01-17 | 1994-09-06 | The Kansai Electric Power Co., Inc. | Process for removing carbon dioxide from combustion exhaust gas |
US5520249A (en) * | 1993-12-23 | 1996-05-28 | Institut Francais Du Petrole | Process for the pretreatment of a natural gas containing hydrogen sulphide |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5397553A (en) * | 1992-10-05 | 1995-03-14 | Electric Power Research Institute, Inc. | Method and apparatus for sequestering carbon dioxide in the deep ocean or aquifers |
-
1998
- 1998-09-24 US US09/159,986 patent/US6149344A/en not_active Ceased
-
2002
- 2002-11-20 US US10/300,265 patent/USRE39077E1/en not_active Expired - Lifetime
-
2004
- 2004-09-09 US US10/937,789 patent/USRE39244E1/en not_active Expired - Lifetime
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3360945A (en) * | 1965-02-25 | 1968-01-02 | Lummus Co | Repressurized natural gas addition to main gas stream to maintain well head pressure |
US4044831A (en) * | 1975-04-02 | 1977-08-30 | Texaco Inc. | Secondary recovery process utilizing water saturated with gas |
US4169133A (en) * | 1977-02-08 | 1979-09-25 | Krupp-Koppers Gmbh | Process for recovering acidic gases collected during gas desulfurization |
US4285917A (en) * | 1980-07-31 | 1981-08-25 | Bayside Holding Corp. | Method for removal of hydrogen sulfide from sour gas streams |
US4449994A (en) * | 1982-01-15 | 1984-05-22 | Air Products And Chemicals, Inc. | Low energy process for separating carbon dioxide and acid gases from a carbonaceous off-gas |
US4576615A (en) * | 1984-08-20 | 1986-03-18 | The Randall Corporation | Carbon dioxide hydrocarbons separation process |
US4848467A (en) * | 1988-02-16 | 1989-07-18 | Conoco Inc. | Formation fracturing process |
US5344627A (en) * | 1992-01-17 | 1994-09-06 | The Kansai Electric Power Co., Inc. | Process for removing carbon dioxide from combustion exhaust gas |
US5340382A (en) * | 1993-07-08 | 1994-08-23 | Beard Thomas L | Acid gas absorption process |
US5520249A (en) * | 1993-12-23 | 1996-05-28 | Institut Francais Du Petrole | Process for the pretreatment of a natural gas containing hydrogen sulphide |
Non-Patent Citations (6)
Title |
---|
Clark, M.A.; Svrcek, W.Y.; Monnery, W.D; Jamaluddin, A.K.M; Bennion, D.B.; Thomas, F.B.; Wicher, E.; Reed, A.D; and Johnson, D.J.; Designing an Optimized Injection Strategy for Acid Gas Disposal Without Dehydration; 77<SUP>th </SUP>Annual GPA Convention, Mar. 16-18, 1998, Dallas, TX. |
Duncan, Grant and Hartford, Catherine A., Operation of Acid Gase Injection/Disposal Wells; World Oil, Oct. 1998, pp. 69-75. |
E. Wichert, Gascan Resources Ltd. and t. Royan, Tartan Engineering Corp. Ltd.; Sulfur Disposal by Acid gas Injection; Apr. 28, 1996. * |
H.L. Longworth, SPE, G.C. Dunn, and M Semchurch; Underground Disposal of acid gas in Alberta Canada; Regulatory concerns and Case Histories; Apr. 26, 1996. * |
Ho, K.T., McMullen, J. Boyle, P., Rojek, O., Forgo, M., Beatty, T. Longworth, H.L.; Subsurface Acid Gas Disposal Scheme in Wayne-Rosedale, Alberta; International Conference on Health, Safety and Environment, Jun. 9-12, 1996, New Orleans, LA; reprinted by Society of Petroleum Engineers, Inc., No. SPE 35848, pp. 691-704. |
Marathon Oil Company Indian Basin Gas Plant Acid Gas Compressor Injection Study AFE 456195; Holloman Corporation; Mar. 27, 1996. |
Cited By (93)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8485252B2 (en) | 2000-04-24 | 2013-07-16 | Shell Oil Company | In situ recovery from a hydrocarbon containing formation |
US8789586B2 (en) | 2000-04-24 | 2014-07-29 | Shell Oil Company | In situ recovery from a hydrocarbon containing formation |
US8225866B2 (en) | 2000-04-24 | 2012-07-24 | Shell Oil Company | In situ recovery from a hydrocarbon containing formation |
US8608249B2 (en) | 2001-04-24 | 2013-12-17 | Shell Oil Company | In situ thermal processing of an oil shale formation |
US8627887B2 (en) | 2001-10-24 | 2014-01-14 | Shell Oil Company | In situ recovery from a hydrocarbon containing formation |
US8230927B2 (en) | 2005-04-22 | 2012-07-31 | Shell Oil Company | Methods and systems for producing fluid from an in situ conversion process |
US8233782B2 (en) | 2005-04-22 | 2012-07-31 | Shell Oil Company | Grouped exposed metal heaters |
US7793722B2 (en) | 2006-04-21 | 2010-09-14 | Shell Oil Company | Non-ferromagnetic overburden casing |
US7673786B2 (en) | 2006-04-21 | 2010-03-09 | Shell Oil Company | Welding shield for coupling heaters |
US8192682B2 (en) | 2006-04-21 | 2012-06-05 | Shell Oil Company | High strength alloys |
US7912358B2 (en) | 2006-04-21 | 2011-03-22 | Shell Oil Company | Alternate energy source usage for in situ heat treatment processes |
US7866385B2 (en) | 2006-04-21 | 2011-01-11 | Shell Oil Company | Power systems utilizing the heat of produced formation fluid |
US8083813B2 (en) | 2006-04-21 | 2011-12-27 | Shell Oil Company | Methods of producing transportation fuel |
US7681647B2 (en) | 2006-10-20 | 2010-03-23 | Shell Oil Company | Method of producing drive fluid in situ in tar sands formations |
US7703513B2 (en) | 2006-10-20 | 2010-04-27 | Shell Oil Company | Wax barrier for use with in situ processes for treating formations |
US8555971B2 (en) | 2006-10-20 | 2013-10-15 | Shell Oil Company | Treating tar sands formations with dolomite |
US8191630B2 (en) | 2006-10-20 | 2012-06-05 | Shell Oil Company | Creating fluid injectivity in tar sands formations |
US7841401B2 (en) | 2006-10-20 | 2010-11-30 | Shell Oil Company | Gas injection to inhibit migration during an in situ heat treatment process |
US7730946B2 (en) | 2006-10-20 | 2010-06-08 | Shell Oil Company | Treating tar sands formations with dolomite |
US7677314B2 (en) | 2006-10-20 | 2010-03-16 | Shell Oil Company | Method of condensing vaporized water in situ to treat tar sands formations |
US7845411B2 (en) | 2006-10-20 | 2010-12-07 | Shell Oil Company | In situ heat treatment process utilizing a closed loop heating system |
US7673681B2 (en) | 2006-10-20 | 2010-03-09 | Shell Oil Company | Treating tar sands formations with karsted zones |
US7730947B2 (en) | 2006-10-20 | 2010-06-08 | Shell Oil Company | Creating fluid injectivity in tar sands formations |
US7730945B2 (en) | 2006-10-20 | 2010-06-08 | Shell Oil Company | Using geothermal energy to heat a portion of a formation for an in situ heat treatment process |
US7717171B2 (en) | 2006-10-20 | 2010-05-18 | Shell Oil Company | Moving hydrocarbons through portions of tar sands formations with a fluid |
US7644765B2 (en) | 2006-10-20 | 2010-01-12 | Shell Oil Company | Heating tar sands formations while controlling pressure |
US7677310B2 (en) | 2006-10-20 | 2010-03-16 | Shell Oil Company | Creating and maintaining a gas cap in tar sands formations |
US7798220B2 (en) | 2007-04-20 | 2010-09-21 | Shell Oil Company | In situ heat treatment of a tar sands formation after drive process treatment |
US7849922B2 (en) | 2007-04-20 | 2010-12-14 | Shell Oil Company | In situ recovery from residually heated sections in a hydrocarbon containing formation |
US9181780B2 (en) | 2007-04-20 | 2015-11-10 | Shell Oil Company | Controlling and assessing pressure conditions during treatment of tar sands formations |
US8327681B2 (en) | 2007-04-20 | 2012-12-11 | Shell Oil Company | Wellbore manufacturing processes for in situ heat treatment processes |
US8459359B2 (en) | 2007-04-20 | 2013-06-11 | Shell Oil Company | Treating nahcolite containing formations and saline zones |
US8042610B2 (en) | 2007-04-20 | 2011-10-25 | Shell Oil Company | Parallel heater system for subsurface formations |
US8381815B2 (en) | 2007-04-20 | 2013-02-26 | Shell Oil Company | Production from multiple zones of a tar sands formation |
US7832484B2 (en) | 2007-04-20 | 2010-11-16 | Shell Oil Company | Molten salt as a heat transfer fluid for heating a subsurface formation |
US8791396B2 (en) | 2007-04-20 | 2014-07-29 | Shell Oil Company | Floating insulated conductors for heating subsurface formations |
US8662175B2 (en) | 2007-04-20 | 2014-03-04 | Shell Oil Company | Varying properties of in situ heat treatment of a tar sands formation based on assessed viscosities |
US7841425B2 (en) | 2007-04-20 | 2010-11-30 | Shell Oil Company | Drilling subsurface wellbores with cutting structures |
US7950453B2 (en) | 2007-04-20 | 2011-05-31 | Shell Oil Company | Downhole burner systems and methods for heating subsurface formations |
US7931086B2 (en) | 2007-04-20 | 2011-04-26 | Shell Oil Company | Heating systems for heating subsurface formations |
US7841408B2 (en) | 2007-04-20 | 2010-11-30 | Shell Oil Company | In situ heat treatment from multiple layers of a tar sands formation |
US8196658B2 (en) | 2007-10-19 | 2012-06-12 | Shell Oil Company | Irregular spacing of heat sources for treating hydrocarbon containing formations |
US8162059B2 (en) | 2007-10-19 | 2012-04-24 | Shell Oil Company | Induction heaters used to heat subsurface formations |
US7866388B2 (en) | 2007-10-19 | 2011-01-11 | Shell Oil Company | High temperature methods for forming oxidizer fuel |
US8113272B2 (en) | 2007-10-19 | 2012-02-14 | Shell Oil Company | Three-phase heaters with common overburden sections for heating subsurface formations |
US8240774B2 (en) | 2007-10-19 | 2012-08-14 | Shell Oil Company | Solution mining and in situ treatment of nahcolite beds |
US8146669B2 (en) | 2007-10-19 | 2012-04-03 | Shell Oil Company | Multi-step heater deployment in a subsurface formation |
US8011451B2 (en) | 2007-10-19 | 2011-09-06 | Shell Oil Company | Ranging methods for developing wellbores in subsurface formations |
US7866386B2 (en) | 2007-10-19 | 2011-01-11 | Shell Oil Company | In situ oxidation of subsurface formations |
US8536497B2 (en) | 2007-10-19 | 2013-09-17 | Shell Oil Company | Methods for forming long subsurface heaters |
US8272455B2 (en) | 2007-10-19 | 2012-09-25 | Shell Oil Company | Methods for forming wellbores in heated formations |
US8276661B2 (en) | 2007-10-19 | 2012-10-02 | Shell Oil Company | Heating subsurface formations by oxidizing fuel on a fuel carrier |
US8146661B2 (en) | 2007-10-19 | 2012-04-03 | Shell Oil Company | Cryogenic treatment of gas |
US20120090838A1 (en) * | 2007-11-06 | 2012-04-19 | Bp Exploration Operating Company Limited | Method of injecting carbon dioxide |
US8622129B2 (en) * | 2007-11-06 | 2014-01-07 | Bp Exploration Operating Company Limited | Method of injecting carbon dioxide |
US8636323B2 (en) | 2008-04-18 | 2014-01-28 | Shell Oil Company | Mines and tunnels for use in treating subsurface hydrocarbon containing formations |
US8562078B2 (en) | 2008-04-18 | 2013-10-22 | Shell Oil Company | Hydrocarbon production from mines and tunnels used in treating subsurface hydrocarbon containing formations |
US9528322B2 (en) | 2008-04-18 | 2016-12-27 | Shell Oil Company | Dual motor systems and non-rotating sensors for use in developing wellbores in subsurface formations |
US8151907B2 (en) | 2008-04-18 | 2012-04-10 | Shell Oil Company | Dual motor systems and non-rotating sensors for use in developing wellbores in subsurface formations |
US8162405B2 (en) | 2008-04-18 | 2012-04-24 | Shell Oil Company | Using tunnels for treating subsurface hydrocarbon containing formations |
US8752904B2 (en) | 2008-04-18 | 2014-06-17 | Shell Oil Company | Heated fluid flow in mines and tunnels used in heating subsurface hydrocarbon containing formations |
US8172335B2 (en) | 2008-04-18 | 2012-05-08 | Shell Oil Company | Electrical current flow between tunnels for use in heating subsurface hydrocarbon containing formations |
US8177305B2 (en) | 2008-04-18 | 2012-05-15 | Shell Oil Company | Heater connections in mines and tunnels for use in treating subsurface hydrocarbon containing formations |
US8256512B2 (en) | 2008-10-13 | 2012-09-04 | Shell Oil Company | Movable heaters for treating subsurface hydrocarbon containing formations |
US8281861B2 (en) | 2008-10-13 | 2012-10-09 | Shell Oil Company | Circulated heated transfer fluid heating of subsurface hydrocarbon formations |
US8353347B2 (en) | 2008-10-13 | 2013-01-15 | Shell Oil Company | Deployment of insulated conductors for treating subsurface formations |
US8220539B2 (en) | 2008-10-13 | 2012-07-17 | Shell Oil Company | Controlling hydrogen pressure in self-regulating nuclear reactors used to treat a subsurface formation |
US8881806B2 (en) | 2008-10-13 | 2014-11-11 | Shell Oil Company | Systems and methods for treating a subsurface formation with electrical conductors |
US8267185B2 (en) | 2008-10-13 | 2012-09-18 | Shell Oil Company | Circulated heated transfer fluid systems used to treat a subsurface formation |
US8267170B2 (en) | 2008-10-13 | 2012-09-18 | Shell Oil Company | Offset barrier wells in subsurface formations |
US9129728B2 (en) | 2008-10-13 | 2015-09-08 | Shell Oil Company | Systems and methods of forming subsurface wellbores |
US8261832B2 (en) | 2008-10-13 | 2012-09-11 | Shell Oil Company | Heating subsurface formations with fluids |
US9051829B2 (en) | 2008-10-13 | 2015-06-09 | Shell Oil Company | Perforated electrical conductors for treating subsurface formations |
US9022118B2 (en) | 2008-10-13 | 2015-05-05 | Shell Oil Company | Double insulated heaters for treating subsurface formations |
US8327932B2 (en) | 2009-04-10 | 2012-12-11 | Shell Oil Company | Recovering energy from a subsurface formation |
US8448707B2 (en) | 2009-04-10 | 2013-05-28 | Shell Oil Company | Non-conducting heater casings |
US8851170B2 (en) | 2009-04-10 | 2014-10-07 | Shell Oil Company | Heater assisted fluid treatment of a subsurface formation |
US8434555B2 (en) | 2009-04-10 | 2013-05-07 | Shell Oil Company | Irregular pattern treatment of a subsurface formation |
US8701768B2 (en) | 2010-04-09 | 2014-04-22 | Shell Oil Company | Methods for treating hydrocarbon formations |
US9127523B2 (en) | 2010-04-09 | 2015-09-08 | Shell Oil Company | Barrier methods for use in subsurface hydrocarbon formations |
US8631866B2 (en) | 2010-04-09 | 2014-01-21 | Shell Oil Company | Leak detection in circulated fluid systems for heating subsurface formations |
US8820406B2 (en) | 2010-04-09 | 2014-09-02 | Shell Oil Company | Electrodes for electrical current flow heating of subsurface formations with conductive material in wellbore |
US9022109B2 (en) | 2010-04-09 | 2015-05-05 | Shell Oil Company | Leak detection in circulated fluid systems for heating subsurface formations |
US9033042B2 (en) | 2010-04-09 | 2015-05-19 | Shell Oil Company | Forming bitumen barriers in subsurface hydrocarbon formations |
US8739874B2 (en) | 2010-04-09 | 2014-06-03 | Shell Oil Company | Methods for heating with slots in hydrocarbon formations |
US9399905B2 (en) | 2010-04-09 | 2016-07-26 | Shell Oil Company | Leak detection in circulated fluid systems for heating subsurface formations |
US9127538B2 (en) | 2010-04-09 | 2015-09-08 | Shell Oil Company | Methodologies for treatment of hydrocarbon formations using staged pyrolyzation |
US8701769B2 (en) | 2010-04-09 | 2014-04-22 | Shell Oil Company | Methods for treating hydrocarbon formations based on geology |
US8833453B2 (en) | 2010-04-09 | 2014-09-16 | Shell Oil Company | Electrodes for electrical current flow heating of subsurface formations with tapered copper thickness |
US20120038174A1 (en) * | 2010-08-13 | 2012-02-16 | Board Of Regents, The University Of Texas System | Storing Carbon Dioxide and Producing Methane and Geothermal Energy from Deep Saline Aquifers |
US9121259B2 (en) * | 2010-08-13 | 2015-09-01 | Board Of Regents, The University Of Texas System | Storing carbon dioxide and producing methane and geothermal energy from deep saline aquifers |
US9016370B2 (en) | 2011-04-08 | 2015-04-28 | Shell Oil Company | Partial solution mining of hydrocarbon containing layers prior to in situ heat treatment |
US9309755B2 (en) | 2011-10-07 | 2016-04-12 | Shell Oil Company | Thermal expansion accommodation for circulated fluid systems used to heat subsurface formations |
Also Published As
Publication number | Publication date |
---|---|
US6149344A (en) | 2000-11-21 |
USRE39077E1 (en) | 2006-04-25 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
USRE39244E1 (en) | Acid gas disposal | |
US3065790A (en) | Oil recovery process | |
Baklid et al. | Sleipner Vest CO2 disposal, CO2 injection into a shallow underground aquifer | |
AU669517B2 (en) | Recovery of natural gases from underground coal formations | |
US6325147B1 (en) | Enhanced oil recovery process with combined injection of an aqueous phase and of at least partially water-miscible gas | |
US11795371B2 (en) | Hydrocarbon based carrier fluid | |
CA2762416C (en) | High pressure hydrocarbon fracturing on demand method and related process | |
EA030629B1 (en) | System for fracturing a formation | |
US5435975A (en) | Process and skid-mounted system for inert gas generation | |
RU2689452C2 (en) | Modular installation for processing flow of composition of reverse inflow and methods for processing it | |
US20170275521A1 (en) | L-grade stimulation fluid | |
WO1991010040A1 (en) | Process for in-situ enrichment of gas used in miscible flooding | |
US4683948A (en) | Enhanced oil recovery process employing carbon dioxide | |
US5340382A (en) | Acid gas absorption process | |
CA2528304A1 (en) | Mobile gas separation unit | |
Sloan | Offshore hydrate engineering handbook | |
Kurz et al. | Upstream and midstream compression applications: Part 1—applications | |
Carroll et al. | Design considerations for acid gas injection | |
US11884877B2 (en) | Method for removing fouling using carbonic acid | |
US20230060929A1 (en) | Method for pumping foamed fluids into a well bore or subterranean formation | |
US3353597A (en) | Formation flooding by sulphur dioxide for recovering oil and gas | |
Dohrn | General correlations for pure-component parameters of two-parameter equations-of-state | |
US20070114024A1 (en) | Anti-oxidizing process for non-cryogenic nitrogen | |
Mearkeltor | Natural Gas Sweetening Process Design | |
US8124824B2 (en) | System and method for using super critical state carbon dioxide (CO2) as a hydrocarbon diluent |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
FPAY | Fee payment |
Year of fee payment: 8 |
|
FPAY | Fee payment |
Year of fee payment: 12 |
|
SULP | Surcharge for late payment |
Year of fee payment: 11 |