CA2281610C - Method and apparatus utilizing hydrocarbon pollutants - Google Patents
Method and apparatus utilizing hydrocarbon pollutants Download PDFInfo
- Publication number
- CA2281610C CA2281610C CA002281610A CA2281610A CA2281610C CA 2281610 C CA2281610 C CA 2281610C CA 002281610 A CA002281610 A CA 002281610A CA 2281610 A CA2281610 A CA 2281610A CA 2281610 C CA2281610 C CA 2281610C
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- hydrocarbons
- uncondensed
- burner
- reboiler
- fuel
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Abstract
An environmentally safe apparatus (10) for reclaiming uncondensed hydrocarbons normally exausted to the atmosphere from the still column (14) of a glycol dehydrator system (12), and utilizing the uncondensed hydrocarbons as fuel in the burner (20) of a reboiler fire-tube (19) by natural draft of the fire-tube exhaust stack (23).
Description
METHOD AND APPARATUS UTILIZING HYDROCARBON
POLLUTANTS
Technical Field 1 This invention relates to glycol dehydrators and more 2 particularly to a method and apparatus which eliminates noxious 3 gasses normally exhausted to the atmosphere from the still 4 column of a gas dehydrator.
Natural gas produced from gas wells contains entrained 6 water and oil droplets, water vapor, and condensable hydrocar-7 bons .
8 It is necessary to remove the water and water vapor from 9 the natural gas before it passes into a pipeline to prevent clogging and corrosion of the pipeline and downstream equip 11 ment .
12 Glycol dehydrators are used to remove water and water 13 vapor from gas by contacting the wet gas with glycol absorbing 14 the water and vapor. The desiccant then flows to a reboiler regenerating the glycol by driving off the water vapor, 16 allowing the reconcentrated desiccant to be returned to the 17 dehydration phase.
18 An unintentional by-product of the dehydration process is 19 the absorption of hydrocarbons with water and water vapor.
1 These hydrocarbons are normally released to the atmosphere with 2 water vapor from the regenerator. Many of these aromatic 3 hydrocarbons are hazardous to the environment, benzene, ethyl-4 benzene, toluene, and xylene for example.
Background Art 6 Some prior patents, such as United States Patent No.
7 3,875,019 issued April 1, 1975 to Cocuzza et al, and United 8 States Patent No. 5,163,981 issued November 17, 1992 to Choi, 9 disclose removing noxious gasses from the vapors emitted by a still column from a reboiler and passing these noxious gasses 11 to the burner of the reboiler. However, a problem occurs in 12 admitting the gasses to the reboiler burner and obtaining 13 combustion since these noxious gasses do not readily burn, as 14 does natural gas. This invention overcomes this problem.
The maj ority of the prior art patents are directed toward 16 the reclaiming and/or reconcentrating ethylene glycol.
17 United States Patent No. 4,273,620 issued June 16, 1981 18 to Knobel, United States Patent No. 4,225,394 issued September 19 30, 1980 to Cox et al, and United States Patent No. 4,322,265 issued March 30, 1982 to Wood, are considered good examples of 21 the further state-of-the-art in reclaiming and reconcentrating 22 used ethylene glycol.
23 Disclosure Of The Invention 24 A glycol dehydrating system includes a reboiler having an upstanding still column receiving vapors having temperatures as 26 high as 177° C. In this invention the still column vent is 27 closed to prevent the normal escape of noxious gasses and water 28 vapor. These vapors are piped through a heat exchanger sized 29 to drop the temperature to less than 66° C. The condensed water and condensable hydrocarbons flow by gravity to tank 31 storage through a self emptying container. The remaining 32 hydrocarbon vapors flow through a secondary separator to remove 33 remaining liquids, and through either of two thermostatically 1 controlled valves for use as dehydrator fuel. In some instal-2 lations, the uncondensed hydrocarbons have been found to be of 3 sufficient quantity to substantially fuel the dehydrator, 4 replacing the natural gas normally used for fuel.
Hrief Description Of The Drawings 6 Figure 1 is a schematic of the apparatus;
7 Figure 2 is a fragmentary side elevational view of a 8 dehydration reboiler fuel and air mixing fire-tube burner inlet 9 tube connected with a noxious gas and air mingle unit;
Figure 3 is a fragmentary exploded isometric view of the 11 noxious gas and air mingle unit, per se; and, 12 Figure 4 is a vertical cross sectional view taken 13 substantially along the line 4---4 of Fig. 2.
14 Best Mode For Carrving,0ut The Invention Referring first to Fig. 1, the reference numeral 10 16 indicates the apparatus as a whole which includes a glycol 17 regenerating apparatus 12 comprising a reboiler 16 having an 18 over temperature controller 15, and a thermostatic temperature 19 controller 17 and having a still column 14 mounted thereon receiving wet glycol from a contactor tower, not shown, via a 21 line 18. The reboiler 16 contains a fire-tube 19 having a 22 burner 20 (Fig. 2), in its burner entrance 19', supplied with 23 fuel gas by a line 21 having a fuel control valve 22 and 24 terminating in an upstanding exhaust stack 23 for heating the glycol.
26 Water vapor and aromatic hydrocarbons vaporized from the 27 wet glycol are normally exhausted to the atmosphere through a 28 vent, not shown, in the wall of the still column 14. However, 29 in this invention, the still column vent is closed, and water vapor and aromatic hydrocarbon gasses pass via a line 26 to an 31 air cooled heat exchanger or vapor condenser 28 where the vapor 32 volume is reduced by condensation.
33 The terms "line" and "piping" as used herein refer to tubular pipes for conducting fluids.
Liquid~r f low by gravi ty f rom the vapor condenser through a drain line 30 to a:z standpipe 3;? which drains to a self emptying liquid conta:ir~er 34 through a check valve 3:5. The upper end portion of t:he standpipe is normally closed by a thermostat controlled fluid pressure valve 31 and a pressure relief valve 33. Air ~~rapor or gas displaced by liquid entering the liquid container ::34 is vented t.o the upper end portion of the stand pipe 32 via:r a line 36. 'The self emptying liquid container 34 is fully disclosed ira United States Patent No.
4,948,010 The container 34 is connected with the fuel gas line 21 via line 37 so that a float, not shown, within the container 34 opens an internal valve, similarly not shown,, when the float is lifted to a predetermined level by contained liquid to allow gas pressure from the line 3'7 to d:isc:harcy=_ contained 3_iquid to storage through a check valve 93 in a drain line 38.
Vapor and aromat.i.c hydra~arbon gasses in the upper end portion of the stand ~:yipe 32 pass to a separator 39 via a line 90. Condensed liquids in the separator drain by gravity through a line 42 to the depending end portion of the stand pipe 32 and to the liquid container 34. Hydrocarbons leaving the separator 39 are filtered by a fi:Yter 48 in a conduit 44 connected to the burner 20 through a no:~r~mally open tehermoetat- control valve 47.
Separated liquids in t:he filter 48 drain to the separator drain line 42 via a line 45~. A flame arrestor 50 is interposed in the conduit 44 downst~.eam from the filter 48. A branch line 55, connected with the t:-ondu~.t 44 upstream from the valve 47 diverts gasses, under c~ertaird conditions as presently ex-plained, to the exhaust stack 23 through a normally closed thermostat controlled v~a:lwe 56.
The over temperature controller 15 is connected with the fuel gas supply :~?1 up~~3t::c.-earn frcnn tkna_ -valv-e~ 22 by a line 13 and C~ _ with the thermostatic temperature control 17 by a line 11.
During normal operation, the teroperature control 17 supplies fuel gas pressure to operate the valves 22, 47 and 56, by gas piping 53, 5'7 arid 58, respeetively_ Other gas piping 59 connects the line 11 <;:o the vent valve 3:1. In the event of reboiler temperature r:~bove a pi:edetermined limit, the over temperature controller :L5 removes gas supply pressure to the thermostat temperature control valve 17 and vent valve 3.L , thus closing fuel and unconciensed hydzo~arbons supply valves 22 and 47 and opening exhaust: stack valve 56 arid vent valve 31.
Referring also to the remaining Figures, the burner 2o is provided with an inlet opening defined by a laterally project-ing boss 60 connected with the fuel line 21. The fuel burner mixer end 62 is open for' admitting air to be mixed with the fuel from the lime 2:L, the qu~intity of air being manually adjusted by a baffle plate 63 can a threaded stem 64.
An aromatic gas and air mingle element 65 is interposed between the burner end 62 and the air inlet control plate 63.
The mingler 65 is provided with a tubular end portion 66 which receives aromatic gasses from the conduit 44. The mingle element 65 has opposing aide walls 68 and 70 provided with axially aligned openings ?2 and 74 surrounding the burner stem 64. The wall forming the side wall opening 72 slidably surrounds the burner stem 64. The side wall 68 is provided with a plurality of radial openings 73, four in the example shown, admitting gas from the mixer 65 to the burner 20. The diameter of the side wall opening 74 is substantially equal with the diameter of the baffle plate 63.
A cylindrical flame arresting element 75 is axially interposed between the burner end c~2 and the mingler side wall 68. A nut 76 on the stem 64 holds the side wall 68 in contact with the adjacent surface of the element 75. In addition to its 1 flame arresting characteristics, the element 75 acts to 2 thoroughly mix or commingle the aromatic gasses with air to 3 form a combustible mixture as they enter the burner 20. A
4 manually operated control valve 67 is interposed in the condui-t 44 downstream from the flame arrestor 50, and a manual bleed 6 valve 69 is interposed in the gas piping 59 upstream from the 7 vent valve 31.
8 As an example, the above described system was installed 9 on a glycol dehydrator and operated for 90 days. The dehydra for has a 375,000 BTU heater, a 76.2 cm contactor, and dries 20 11 mmcf natural gas per day. Gas temperature is 43° C. Contactor 12 pressure is 1,000 psi. Total liquid hydrocarbons recovered, 13 3.33 bbls/day x 90 = 299.7 bbls. Total natural gas fuel saved 14 by using the aromatic hydrocarbons as fuel is: 18 mcf/day x 90 = 1.620 mmcf.
16 Under normal conditions the apparatus continuously 17 operates under a predetermined temperature controlled by the 18 temperature controller 17. In the event of a malfunction, such 19 as the temperature rising or falling to a temperature range beyond the setting of the temperature control, the over temp-21 erature controller 15 closes the burner valve 22 and uncon-22 densed hydrocarbon gas valve 47 and opens the uncondensed 23 hydrocarbon gas valve 56 to the exhaust stack 23 and opens the 24 vent valve 31 to atmosphere. Uncondensed hydrocarbon gasses diverted to the exhaust stack are mingled with a thermal draft 26 in the presence of an igniter, not shown.
27 Obviously the invention is susceptible to changes or 28 alterations without defeating its practicability. Therefore, 29 we do not wish to be confined to the preferred embodiment shown in the drawings and described herein.
POLLUTANTS
Technical Field 1 This invention relates to glycol dehydrators and more 2 particularly to a method and apparatus which eliminates noxious 3 gasses normally exhausted to the atmosphere from the still 4 column of a gas dehydrator.
Natural gas produced from gas wells contains entrained 6 water and oil droplets, water vapor, and condensable hydrocar-7 bons .
8 It is necessary to remove the water and water vapor from 9 the natural gas before it passes into a pipeline to prevent clogging and corrosion of the pipeline and downstream equip 11 ment .
12 Glycol dehydrators are used to remove water and water 13 vapor from gas by contacting the wet gas with glycol absorbing 14 the water and vapor. The desiccant then flows to a reboiler regenerating the glycol by driving off the water vapor, 16 allowing the reconcentrated desiccant to be returned to the 17 dehydration phase.
18 An unintentional by-product of the dehydration process is 19 the absorption of hydrocarbons with water and water vapor.
1 These hydrocarbons are normally released to the atmosphere with 2 water vapor from the regenerator. Many of these aromatic 3 hydrocarbons are hazardous to the environment, benzene, ethyl-4 benzene, toluene, and xylene for example.
Background Art 6 Some prior patents, such as United States Patent No.
7 3,875,019 issued April 1, 1975 to Cocuzza et al, and United 8 States Patent No. 5,163,981 issued November 17, 1992 to Choi, 9 disclose removing noxious gasses from the vapors emitted by a still column from a reboiler and passing these noxious gasses 11 to the burner of the reboiler. However, a problem occurs in 12 admitting the gasses to the reboiler burner and obtaining 13 combustion since these noxious gasses do not readily burn, as 14 does natural gas. This invention overcomes this problem.
The maj ority of the prior art patents are directed toward 16 the reclaiming and/or reconcentrating ethylene glycol.
17 United States Patent No. 4,273,620 issued June 16, 1981 18 to Knobel, United States Patent No. 4,225,394 issued September 19 30, 1980 to Cox et al, and United States Patent No. 4,322,265 issued March 30, 1982 to Wood, are considered good examples of 21 the further state-of-the-art in reclaiming and reconcentrating 22 used ethylene glycol.
23 Disclosure Of The Invention 24 A glycol dehydrating system includes a reboiler having an upstanding still column receiving vapors having temperatures as 26 high as 177° C. In this invention the still column vent is 27 closed to prevent the normal escape of noxious gasses and water 28 vapor. These vapors are piped through a heat exchanger sized 29 to drop the temperature to less than 66° C. The condensed water and condensable hydrocarbons flow by gravity to tank 31 storage through a self emptying container. The remaining 32 hydrocarbon vapors flow through a secondary separator to remove 33 remaining liquids, and through either of two thermostatically 1 controlled valves for use as dehydrator fuel. In some instal-2 lations, the uncondensed hydrocarbons have been found to be of 3 sufficient quantity to substantially fuel the dehydrator, 4 replacing the natural gas normally used for fuel.
Hrief Description Of The Drawings 6 Figure 1 is a schematic of the apparatus;
7 Figure 2 is a fragmentary side elevational view of a 8 dehydration reboiler fuel and air mixing fire-tube burner inlet 9 tube connected with a noxious gas and air mingle unit;
Figure 3 is a fragmentary exploded isometric view of the 11 noxious gas and air mingle unit, per se; and, 12 Figure 4 is a vertical cross sectional view taken 13 substantially along the line 4---4 of Fig. 2.
14 Best Mode For Carrving,0ut The Invention Referring first to Fig. 1, the reference numeral 10 16 indicates the apparatus as a whole which includes a glycol 17 regenerating apparatus 12 comprising a reboiler 16 having an 18 over temperature controller 15, and a thermostatic temperature 19 controller 17 and having a still column 14 mounted thereon receiving wet glycol from a contactor tower, not shown, via a 21 line 18. The reboiler 16 contains a fire-tube 19 having a 22 burner 20 (Fig. 2), in its burner entrance 19', supplied with 23 fuel gas by a line 21 having a fuel control valve 22 and 24 terminating in an upstanding exhaust stack 23 for heating the glycol.
26 Water vapor and aromatic hydrocarbons vaporized from the 27 wet glycol are normally exhausted to the atmosphere through a 28 vent, not shown, in the wall of the still column 14. However, 29 in this invention, the still column vent is closed, and water vapor and aromatic hydrocarbon gasses pass via a line 26 to an 31 air cooled heat exchanger or vapor condenser 28 where the vapor 32 volume is reduced by condensation.
33 The terms "line" and "piping" as used herein refer to tubular pipes for conducting fluids.
Liquid~r f low by gravi ty f rom the vapor condenser through a drain line 30 to a:z standpipe 3;? which drains to a self emptying liquid conta:ir~er 34 through a check valve 3:5. The upper end portion of t:he standpipe is normally closed by a thermostat controlled fluid pressure valve 31 and a pressure relief valve 33. Air ~~rapor or gas displaced by liquid entering the liquid container ::34 is vented t.o the upper end portion of the stand pipe 32 via:r a line 36. 'The self emptying liquid container 34 is fully disclosed ira United States Patent No.
4,948,010 The container 34 is connected with the fuel gas line 21 via line 37 so that a float, not shown, within the container 34 opens an internal valve, similarly not shown,, when the float is lifted to a predetermined level by contained liquid to allow gas pressure from the line 3'7 to d:isc:harcy=_ contained 3_iquid to storage through a check valve 93 in a drain line 38.
Vapor and aromat.i.c hydra~arbon gasses in the upper end portion of the stand ~:yipe 32 pass to a separator 39 via a line 90. Condensed liquids in the separator drain by gravity through a line 42 to the depending end portion of the stand pipe 32 and to the liquid container 34. Hydrocarbons leaving the separator 39 are filtered by a fi:Yter 48 in a conduit 44 connected to the burner 20 through a no:~r~mally open tehermoetat- control valve 47.
Separated liquids in t:he filter 48 drain to the separator drain line 42 via a line 45~. A flame arrestor 50 is interposed in the conduit 44 downst~.eam from the filter 48. A branch line 55, connected with the t:-ondu~.t 44 upstream from the valve 47 diverts gasses, under c~ertaird conditions as presently ex-plained, to the exhaust stack 23 through a normally closed thermostat controlled v~a:lwe 56.
The over temperature controller 15 is connected with the fuel gas supply :~?1 up~~3t::c.-earn frcnn tkna_ -valv-e~ 22 by a line 13 and C~ _ with the thermostatic temperature control 17 by a line 11.
During normal operation, the teroperature control 17 supplies fuel gas pressure to operate the valves 22, 47 and 56, by gas piping 53, 5'7 arid 58, respeetively_ Other gas piping 59 connects the line 11 <;:o the vent valve 3:1. In the event of reboiler temperature r:~bove a pi:edetermined limit, the over temperature controller :L5 removes gas supply pressure to the thermostat temperature control valve 17 and vent valve 3.L , thus closing fuel and unconciensed hydzo~arbons supply valves 22 and 47 and opening exhaust: stack valve 56 arid vent valve 31.
Referring also to the remaining Figures, the burner 2o is provided with an inlet opening defined by a laterally project-ing boss 60 connected with the fuel line 21. The fuel burner mixer end 62 is open for' admitting air to be mixed with the fuel from the lime 2:L, the qu~intity of air being manually adjusted by a baffle plate 63 can a threaded stem 64.
An aromatic gas and air mingle element 65 is interposed between the burner end 62 and the air inlet control plate 63.
The mingler 65 is provided with a tubular end portion 66 which receives aromatic gasses from the conduit 44. The mingle element 65 has opposing aide walls 68 and 70 provided with axially aligned openings ?2 and 74 surrounding the burner stem 64. The wall forming the side wall opening 72 slidably surrounds the burner stem 64. The side wall 68 is provided with a plurality of radial openings 73, four in the example shown, admitting gas from the mixer 65 to the burner 20. The diameter of the side wall opening 74 is substantially equal with the diameter of the baffle plate 63.
A cylindrical flame arresting element 75 is axially interposed between the burner end c~2 and the mingler side wall 68. A nut 76 on the stem 64 holds the side wall 68 in contact with the adjacent surface of the element 75. In addition to its 1 flame arresting characteristics, the element 75 acts to 2 thoroughly mix or commingle the aromatic gasses with air to 3 form a combustible mixture as they enter the burner 20. A
4 manually operated control valve 67 is interposed in the condui-t 44 downstream from the flame arrestor 50, and a manual bleed 6 valve 69 is interposed in the gas piping 59 upstream from the 7 vent valve 31.
8 As an example, the above described system was installed 9 on a glycol dehydrator and operated for 90 days. The dehydra for has a 375,000 BTU heater, a 76.2 cm contactor, and dries 20 11 mmcf natural gas per day. Gas temperature is 43° C. Contactor 12 pressure is 1,000 psi. Total liquid hydrocarbons recovered, 13 3.33 bbls/day x 90 = 299.7 bbls. Total natural gas fuel saved 14 by using the aromatic hydrocarbons as fuel is: 18 mcf/day x 90 = 1.620 mmcf.
16 Under normal conditions the apparatus continuously 17 operates under a predetermined temperature controlled by the 18 temperature controller 17. In the event of a malfunction, such 19 as the temperature rising or falling to a temperature range beyond the setting of the temperature control, the over temp-21 erature controller 15 closes the burner valve 22 and uncon-22 densed hydrocarbon gas valve 47 and opens the uncondensed 23 hydrocarbon gas valve 56 to the exhaust stack 23 and opens the 24 vent valve 31 to atmosphere. Uncondensed hydrocarbon gasses diverted to the exhaust stack are mingled with a thermal draft 26 in the presence of an igniter, not shown.
27 Obviously the invention is susceptible to changes or 28 alterations without defeating its practicability. Therefore, 29 we do not wish to be confined to the preferred embodiment shown in the drawings and described herein.
Claims (12)
1. In a method for recovering water and aromatic hydrocarbons evaporated from glycol in a still column mounted on a reboiler, having a fire-tube provided with a fuel intake for receiving a fuel under pressure and a combustion air intake, in a glycol regenerating apparatus, the improvement comprising:
(a) passing water and hydrocarbons vapor from said still column to a vapor condenser;
(b) passing uncondensed vapors from said vapor condensor to a condensate separator; and (c) entraining non-condensable hydrocarbon vapors from said condensate separator directly into a combustion air stream at the combustion air intake of the fire-tube in said reboiler, whereby the only gaseous discharge from the reboiler regenerating apparatus is combustion products from the reboiler fire-tube.
(a) passing water and hydrocarbons vapor from said still column to a vapor condenser;
(b) passing uncondensed vapors from said vapor condensor to a condensate separator; and (c) entraining non-condensable hydrocarbon vapors from said condensate separator directly into a combustion air stream at the combustion air intake of the fire-tube in said reboiler, whereby the only gaseous discharge from the reboiler regenerating apparatus is combustion products from the reboiler fire-tube.
2. The method of claim 1, wherein the non-condensable hydrocarbon vapors from said condensate separator are passed through a hydrocarbon vapor and air mingler at the combustion air intake for entraining the vapors with the combustion air.
3. The method of claim 2, comprising the additional step of using the fuel pressure for forcing uncondensed vapors from said condensate separator to the hydrocarbon vapor and air mingler.
4. The method of claim 3, including the further step of passing effluent from said vapor condenser and said separator to a self emptying container.
5. The method of claim 4, including the further step of applying the fuel pressure to the container for forcing evacuation of liquids contained therein.
6. The method of claim 1, wherein said vapor condenser is an air cooled condenser.
7. An apparatus for recovering water and aromatic hydrocarbons evaporated from glycol in a glycol regenerator including a still column, a reboiler section having a burner and a fire-tube with a burner end portion including a fuel intake for receiving a fuel under pressure and a combustion air intake, and an exhaust stack end portion extending therefrom, the regenerator further including an over temperature controller and a thermostat temperature control on the reboiler section, the apparatus comprising:
a water and hydrocarbon gas vapor condenser for receiving vapors from the still column and including separate outlets for condensed water and hydrocarbons, and uncondensed hydrocarbons;
an uncondensed hydrocarbons separator downstream from said vapor condenser and having separate outlets for water and condensed hydrocarbons and uncondensed hydrocarbons;
a supply conduit extending from said separator uncondensed hydrocarbons outlet for conveying uncondensed hydrocarbons to said burner; and means for entraining the uncondensed hydrocarbons received from the supply conduit directly with combustion air at the combustion air intake for forming a combustible mixture entering said burner.
a water and hydrocarbon gas vapor condenser for receiving vapors from the still column and including separate outlets for condensed water and hydrocarbons, and uncondensed hydrocarbons;
an uncondensed hydrocarbons separator downstream from said vapor condenser and having separate outlets for water and condensed hydrocarbons and uncondensed hydrocarbons;
a supply conduit extending from said separator uncondensed hydrocarbons outlet for conveying uncondensed hydrocarbons to said burner; and means for entraining the uncondensed hydrocarbons received from the supply conduit directly with combustion air at the combustion air intake for forming a combustible mixture entering said burner.
8. The apparatus of claim 7, further including means for forcing the uncondensed hydrocarbons by way of the fuel pressure through the supply conduit to the burner.
9. The apparatus of claim 8, wherein the means for forcing is a pressure conduit connecting a pressurized fuel supply of the burner with the separator.
10. The apparatus of claim 7, wherein the means for entraining is an air and uncondensed hydrocarbons mingler interposed between said supply conduit and said burner.
11. The apparatus of claim 7, further comprising a self emptying to storage liquid receiving container downstream from the water and condensed hydrocarbons outlets of said vapor condenser and said separator.
12. The apparatus according to claim 7, further comprising:
a first normally closed valve on said vapor condenser outlet upstream from the uncondensed hydrocarbons outlet;
a second normally open valve interposed in said conduit;
a third normally closed valve and tubing interposed between said conduit and said reboiler exhaust stack upstream from said second valve; and, reboiler fuel gas piping means connecting said temperature controller with said first, second and third valves for opening said first and third valves and closing said second valve, respectively, in response to a temperature malfunction.
a first normally closed valve on said vapor condenser outlet upstream from the uncondensed hydrocarbons outlet;
a second normally open valve interposed in said conduit;
a third normally closed valve and tubing interposed between said conduit and said reboiler exhaust stack upstream from said second valve; and, reboiler fuel gas piping means connecting said temperature controller with said first, second and third valves for opening said first and third valves and closing said second valve, respectively, in response to a temperature malfunction.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/US1997/003295 WO1998039078A1 (en) | 1995-12-12 | 1997-03-03 | Method and apparatus utilizing hydrocarbon pollutants |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2281610A1 CA2281610A1 (en) | 1998-09-11 |
| CA2281610C true CA2281610C (en) | 2004-06-22 |
Family
ID=31493990
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002281610A Expired - Lifetime CA2281610C (en) | 1997-03-03 | 1997-03-03 | Method and apparatus utilizing hydrocarbon pollutants |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2281610C (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8529215B2 (en) | 2008-03-06 | 2013-09-10 | Rodney T. Heath | Liquid hydrocarbon slug containing vapor recovery system |
| US8864887B2 (en) | 2010-09-30 | 2014-10-21 | Rodney T. Heath | High efficiency slug containing vapor recovery |
| TWI507241B (en) * | 2009-10-26 | 2015-11-11 | Chiyoda Corp | Exhaust gas treatment device |
| US9291409B1 (en) | 2013-03-15 | 2016-03-22 | Rodney T. Heath | Compressor inter-stage temperature control |
| US9353315B2 (en) | 2004-09-22 | 2016-05-31 | Rodney T. Heath | Vapor process system |
| US9527786B1 (en) | 2013-03-15 | 2016-12-27 | Rodney T. Heath | Compressor equipped emissions free dehydrator |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7905722B1 (en) | 2002-02-08 | 2011-03-15 | Heath Rodney T | Control of an adjustable secondary air controller for a burner |
| WO2013170190A1 (en) | 2012-05-10 | 2013-11-14 | Heath Rodney T | Treater combination unit |
| US9932989B1 (en) | 2013-10-24 | 2018-04-03 | Rodney T. Heath | Produced liquids compressor cooler |
-
1997
- 1997-03-03 CA CA002281610A patent/CA2281610C/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9353315B2 (en) | 2004-09-22 | 2016-05-31 | Rodney T. Heath | Vapor process system |
| US8529215B2 (en) | 2008-03-06 | 2013-09-10 | Rodney T. Heath | Liquid hydrocarbon slug containing vapor recovery system |
| US8840703B1 (en) | 2008-03-06 | 2014-09-23 | Rodney T. Heath | Liquid hydrocarbon slug containing vapor recovery system |
| US8900343B1 (en) | 2008-03-06 | 2014-12-02 | Rodney T. Heath | Liquid hydrocarbon slug containing vapor recovery system |
| TWI507241B (en) * | 2009-10-26 | 2015-11-11 | Chiyoda Corp | Exhaust gas treatment device |
| US8864887B2 (en) | 2010-09-30 | 2014-10-21 | Rodney T. Heath | High efficiency slug containing vapor recovery |
| US9291409B1 (en) | 2013-03-15 | 2016-03-22 | Rodney T. Heath | Compressor inter-stage temperature control |
| US9527786B1 (en) | 2013-03-15 | 2016-12-27 | Rodney T. Heath | Compressor equipped emissions free dehydrator |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2281610A1 (en) | 1998-09-11 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKEX | Expiry |
Effective date: 20170303 |