WO2010019510A2 - Mercury removal from crude oil - Google Patents
Mercury removal from crude oil Download PDFInfo
- Publication number
- WO2010019510A2 WO2010019510A2 PCT/US2009/053292 US2009053292W WO2010019510A2 WO 2010019510 A2 WO2010019510 A2 WO 2010019510A2 US 2009053292 W US2009053292 W US 2009053292W WO 2010019510 A2 WO2010019510 A2 WO 2010019510A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- stream
- gas stream
- treated
- mercury
- liquid
- Prior art date
Links
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 title claims abstract description 119
- 229910052753 mercury Inorganic materials 0.000 title claims abstract description 104
- 239000010779 crude oil Substances 0.000 title claims abstract description 35
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 103
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 103
- 239000007788 liquid Substances 0.000 claims abstract description 99
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 92
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000000034 method Methods 0.000 claims abstract description 29
- 239000003345 natural gas Substances 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims description 104
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 20
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 11
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 10
- 239000001294 propane Substances 0.000 claims description 10
- 239000001273 butane Substances 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 6
- 238000012856 packing Methods 0.000 claims description 6
- 238000012546 transfer Methods 0.000 claims description 6
- 239000002594 sorbent Substances 0.000 claims description 2
- 238000012545 processing Methods 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 12
- DIOQZVSQGTUSAI-UHFFFAOYSA-N decane Chemical compound CCCCCCCCCC DIOQZVSQGTUSAI-UHFFFAOYSA-N 0.000 description 10
- 239000000203 mixture Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 238000010521 absorption reaction Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 235000013844 butane Nutrition 0.000 description 5
- 238000002474 experimental method Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 238000004088 simulation Methods 0.000 description 5
- 238000004364 calculation method Methods 0.000 description 4
- 125000004432 carbon atom Chemical group C* 0.000 description 4
- 239000012043 crude product Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000011143 downstream manufacturing Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000005094 computer simulation Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002731 mercury compounds Chemical class 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000741 silica gel Substances 0.000 description 1
- 229910002027 silica gel Inorganic materials 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
-
- 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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/64—Heavy metals or compounds thereof, e.g. mercury
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/60—Heavy metals or heavy metal compounds
- B01D2257/602—Mercury or mercury compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/401—Further details for adsorption processes and devices using a single bed
Definitions
- Embodiments of the invention relate to processes for removal of mercury from crude oil.
- a process of removing mercury from crude oil includes separating a crude oil stream into a gaseous hydrocarbon stream and a liquid hydrocarbon stream and removing mercury from the gaseous hydrocarbon stream to provide a treated gas stream. Contacting the treated gas stream with the liquid hydrocarbon stream transfers mercury from the liquid hydrocarbon stream to the treated gas stream and thereby forms a treated liquid stream and a mercury rich gas stream. The method further includes removing mercury from the mercury rich gas stream.
- a process includes transferring mercury from a liquid hydrocarbon stream to a natural gas stream. The transferring occurs by contacting the liquid hydrocarbon stream with the natural gas stream to thereby form a treated liquid stream and a mercury rich gas stream.
- the method includes removing mercury from the mercury rich gas stream.
- a process includes separating a crude oil stream into a gaseous hydrocarbon stream and a liquid hydrocarbon stream, removing mercury from the gaseous hydrocarbon stream to provide a treated gas stream, and introducing the treated gas stream into contact with the liquid hydrocarbon stream to transfer mercury from the liquid hydrocarbon stream to the treated gas stream and thereby form a treated liquid stream and a mercury rich gas stream.
- Separating the treated gas stream to remove propane and butane from the treated gas stream occurs prior to contacting the treated gas stream with the liquid hydrocarbon stream.
- Introducing a pentane-plus vapor stream separated from the treated gas stream into contact with the treated liquid stream enables absorbing the pentane-plus vapor stream into the treated liquid stream.
- Removing mercury from the mercury rich gas stream provides recycled gas that provides part of the treated gas stream.
- Figure 1 is a simplified schematic flow diagram of an assembly for removing mercury from crude oil, according to one embodiment.
- Figure 2 is a simplified schematic flow diagram of another assembly for removing mercury from crude oil, according to one embodiment.
- Figure 3 is a graphic illustration of a temperature versus pressure curve, resulting from a simulation, above which temperature 90% mercury removal from a crude oil is predicted.
- Figure 4 is a graphic illustration of results from experiments concerning the removal of mercury from decane using methane as a sparging media.
- Figure 5 is a simplified schematic flow diagram of an assembly for removing mercury from crude oil and absorbing hydrocarbon vapors back into the crude oil, according to one embodiment.
- Figure 6 is a graphic illustration of computer simulation results of ratio of mercury in liquid product to mercury in liquid feed versus number of theoretical stages in a gas/liquid contactor used for removing mercury, according to one embodiment.
- Embodiments of the invention relate to removal of mercury from crude oil. Such removal relies on transferring mercury from a liquid hydrocarbon stream to a natural gas stream upon contacting the liquid hydrocarbon stream with the natural gas stream. Processing of the natural gas stream after used to strip the mercury from the liquid hydrocarbon stream removes the mercury from the natural gas stream.
- the removal of the mercury from the crude oil provides marketable products and can be performed onsite at well locations, such as offshore platforms with limited space and facilities, prior to transport to refineries. For example, initial production may contain concentrations of mercury above acceptable thresholds or penalty levels for the refineries such that the removal of the mercury reduces or eliminates penalties and otherwise makes the products marketable.
- Figure 1 illustrates a system in which crude oil is removed from a crude oil well by line 100 and is passed to a separator 102 for separation into a gaseous hydrocarbon stream comprising, consisting of, or consisting essentially of hydrocarbons, mercury and water, which is removed from the separator 102 by line 104, and into a liquid hydrocarbon stream: 1) comprising, consisting of, or consisting essentially of hydrocarbons and elemental mercury, or 2) comprising, consisting of, or consisting essentially of hydrocarbons, elemental mercury and water, which is removed from the separator 102 by line 106.
- a mercury-containing gas feed including in part at least a portion of the gaseous hydrocarbon stream, is charged to a mercury removal unit (MRU) 108 by line 110 for removal of mercury from the mercury-containing gas feed, thereby forming a treated gas stream, which is removed from the MRU 108 by line 112.
- a recycle gas stream comprising a portion of the treated gas stream from the line 112 is charged to a contactor 114 by line 116 for contact with at least a portion of the liquid hydrocarbon stream charged to the contactor 114 by the line 106.
- the elemental mercury contained in the liquid hydrocarbon stream is transferred to the recycle gas stream, thereby forming a mercury rich gas stream, which is removed from the contactor 114 by line 118, and a treated liquid hydrocarbon stream, which is removed from the contactor 114 by line 120.
- the mercury rich gas stream is passed to the MRU 108 as a portion of the mercury- containing gas feed by the lines 118 and 110.
- the contactor 114 includes multiple (e.g., 2, 4, 6 or more) theoretical stages 122 (depicted by "X" within the contactor 114) of separation between vapor and liquid phases. Either trays or packing material in a flow path of fluids described herein passing through the contactor 114 may form the theoretical stages 122.
- the packing material disposed inside of the contactor 114 to define the stages 122 may include random oriented objects or a shaped structure and may be made of metallic or ceramic solid material. In some embodiments, amount of the packing material utilized depends on a desired number of the stages 122 provided by the packing material.
- Figure 2 shows a system in which crude oil is removed from a crude oil well by line 200 and is passed to a first separator 202 for separation into a gaseous hydrocarbon stream comprising, consisting of, or consisting essentially of hydrocarbons, mercury and water, which is removed from the first separator 202 by line 204, and into a liquid hydrocarbon stream comprising, consisting of, or consisting essentially of hydrocarbons, elemental mercury and water, which is removed from the separator 202 by line 206.
- the gaseous hydrocarbon stream is charged to a second separator 207 wherein water is removed and exits the second separator 207 by line 208.
- Overhead gases leaving the second separator 207 by line 209 are charged to a mercury removal unit (MRU) 210 as a mercury-containing gas feed for removal of mercury from the mercury-containing gas feed, thereby forming a treated gas stream, which is removed from the MRU 210 by line 212.
- a recycle gas stream comprising a portion of the treated gas stream from line 212 is charged to a contactor 214 by line 216 for contact with at least a portion of the liquid hydrocarbon stream charged to the contactor 214 by the line 206.
- the elemental mercury contained in the liquid hydrocarbon stream is transferred to the recycle gas stream, thereby forming a mercury rich gas stream, which is removed from the contactor 214 by line 218, and a treated liquid hydrocarbon stream, which is removed from the contactor 214 by line 220.
- the mercury rich gas stream is passed to the second separator 207 along with the gaseous hydrocarbon stream by the lines 218 and 204.
- water is separated from the liquid hydrocarbon stream (and from the recycle gas stream, if water is present in such) and removed from the contactor 214 by line 222.
- a third separator is included in between the first separator 202 and the contactor 214 to separate water from the liquid hydrocarbon stream 206.
- FIG. 5 illustrates a system that includes a separator 602, a MRU 608 and a contactor 614, which operate to remove mercury from a crude oil stream as described herein.
- another separator is included in between the separator 602 and the contactor 614 to separate water from the liquid hydrocarbon stream.
- the system further includes a compression and recovery unit 650, a dryer 652, a gas separating unit 654 and a condenser 656 coupled together to facilitate processing associated with removal of the mercury.
- the dryer 652 removes water vapor from the gasses that pass through the MRU
- the gas separating unit 654 separates the gasses treated in the MRU 608 into: 1) a propane stream denoted as C3, 2) a butanes stream depicted as C4, 3) a product gas stream 616 that includes methane and ethane (C1-C2), and 4) a pentane-plus gas stream that feeds into the condenser 656 and includes hydrocarbons having at least five carbon atoms per molecule.
- a portion of the product gas stream 616 enters into a stripping zone 613 of the contactor 614 to achieve the removal of mercury from liquids passing through the contactor 614.
- any portion or all of the product gas stream 616 introduced into the stripping zone 613 may bypass separation (i.e., removal of propane, butane and/or pentane-plus) and still achieve mercury and/or propane and butane stripping from the liquids passing through the stripping zone 613 of the contactor 614 as described herein.
- the pentane-plus gas stream introduced into the condenser 656 condenses and is separated into vapors that include pentanes and higher molecular weight hydrocarbons output from the condenser 656 as a blend component stream 657 and liquids (identified as C5+) including hydrocarbons having at least five carbon atoms per molecule. At least a portion of the blend component stream 657 enters into an absorption zone 615 contained in the contactor 614 for transfer of at least a portion of the vapors within the blend component stream 657 to a treated liquid hydrocarbon stream from the stripping zone 613, thereby forming an enriched treated liquid hydrocarbon stream.
- the absorption zone 615 provides contact surface area, mixing and residence time sufficient (e.g., via packing material and/or trays shown in figure 5) to absorb at least a portion of the pentanes and higher molecular weight hydrocarbons contained in the blend component stream 657 into the treated liquid hydrocarbon stream.
- the absorption zone 615 is located in the contactor 614 at a location below the stripping zone 613 such that the treated liquid hydrocarbon stream flows from the stripping zone 613 to the absorption zone 615.
- the enriched treated liquid hydrocarbon stream provides crude product removed from the contactor 614.
- the crude oil stream in some embodiments comprises, consists of, or consists essentially of a broad range crude oil.
- the crude oil stream may include hydrocarbons containing at least one carbon atom per molecule.
- the gaseous hydrocarbon stream comprises, consists of, or consists essentially of hydrocarbons containing from about 1 to about 6 carbon atoms per molecule.
- the temperature at which the crude oil stream is separated into the gaseous hydrocarbon stream and the liquid hydrocarbon stream is at least about 50 0 C or at least about 60 0 C.
- the pressure at which the crude oil stream is separated into the gaseous hydrocarbon stream and the liquid hydrocarbon stream is at least about 0.5 Bars or at least about 1 Bars, for some embodiments.
- the mercury removal unit has a fixed bed comprising any mercury sorbent material capable of removing mercury from gases
- the treated gas stream comprises less than about 20 wt. % of the mercury contained in the mercury-containing gas feed or less than about 10 wt. % of the mercury contained in the mercury-containing gas feed.
- the treated liquid hydrocarbon stream may comprise less than about 50 wt. % of the elemental mercury contained in the liquid hydrocarbon stream or less than about 20 wt. % of the elemental mercury contained in the liquid hydrocarbon stream.
- the liquid hydrocarbon stream for some embodiments comprises at least about 10 ppb elemental mercury or comprises at least about 200 ppb elemental mercury.
- the recycle gas stream is contacted with the liquid hydrocarbon stream at a temperature in the range of from about 70 0 C to about 300 0 C or from about 150 0 C to about 200 0 C; a pressure in the range of from about 0.5 Bars to about 15 Bars, from about IBar to about 10
- gas/oil contactor ranges from about ⁇ 1 to ⁇ 3 Bars.
- reservoir temperature of high mercury crude oils is greater than about
- Various vapor/liquid (V/L) molar ratios of gas to hydrocarbon liquid were used in the simulations (0.295, 0.147 and 0.074). Results of the model are shown in Figure 6 and demonstrate that for all V/L molar ratios increasing the number of theoretical stages results in increased mercury removal. For instance, increasing the number of theoretical stages from 1 to 5 increased the mercury removal by a factor of four.
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Abstract
Methods and apparatus relate to removal of mercury from crude oil. Such removal relies on transferring mercury from a liquid hydrocarbon stream to a natural gas stream upon contacting the liquid hydrocarbon stream with the natural gas stream. Processing of the natural gas stream after used to strip the mercury from the liquid hydrocarbon stream removes the mercury from the natural gas stream.
Description
THE UNITED STATES PATENT AND TRADEMARK OFFICE APPLICATION FOR UNITED STATES LETTERS PATENT
MERCURY REMOVAL FROM CRUDE OIL
By:
Joseph B, Cross
Probjot Singh
Richard D. Sadok
Howard L. Wilson
John M. Hays
MERCURY REMOVAL FROM CRUDE OIL
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application is a contimiation-in-part of United States Patent Application
Serial Number 12/174,816, filed August 11, 2008, which is herein incorporated by reference.
STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR
DEVELOPMENT
[0002] None
FIELD OF THE INVENTION
[0003] Embodiments of the invention relate to processes for removal of mercury from crude oil.
BACKGROUND OF THE INVENTION
[0004] Presence of mercury in crude oil can cause problems with downstream processing units as well as health and environmental issues. Such concerns provide incentives to remove the mercury from the crude oil. Therefore, there exists a need for improved processes of removing mercury from crude oil before downstream processing into products.
SUMMARY OF THE INVENTION
[0005] In one embodiment, a process of removing mercury from crude oil includes separating a crude oil stream into a gaseous hydrocarbon stream and a liquid hydrocarbon stream and removing mercury from the gaseous hydrocarbon stream to provide a treated gas stream. Contacting the treated gas stream with the liquid hydrocarbon stream transfers mercury from the liquid hydrocarbon stream to the treated gas stream and thereby forms a treated liquid stream and a mercury rich gas stream. The method further includes removing mercury from the mercury rich gas stream.
[0006] According to one embodiment, a process includes transferring mercury from a liquid hydrocarbon stream to a natural gas stream. The transferring occurs by contacting the liquid hydrocarbon stream with the natural gas stream to thereby form a treated liquid stream and a mercury rich gas stream. In addition, the method includes removing mercury from the mercury rich gas stream.
[0007] For one embodiment, a process includes separating a crude oil stream into a gaseous hydrocarbon stream and a liquid hydrocarbon stream, removing mercury from the gaseous hydrocarbon stream to provide a treated gas stream, and introducing the treated gas stream into contact with the liquid hydrocarbon stream to transfer mercury from the liquid hydrocarbon stream to the treated gas stream and thereby form a treated liquid stream and a mercury rich gas stream. Separating the treated gas stream to remove propane and butane from the treated gas stream occurs prior to contacting the treated gas stream with the liquid hydrocarbon stream. Introducing a pentane-plus vapor stream separated from the treated gas stream into contact with the treated liquid stream enables absorbing the pentane-plus vapor stream into the treated liquid stream. Removing mercury from the mercury rich gas stream provides recycled gas that provides part of the treated gas stream.
BRIEF DESCRIPTION OF THE DRAWINGS
[0008] The invention, together with further advantages thereof, may best be understood by reference to the following description taken in conjunction with the accompanying drawings. [0009] Figure 1 is a simplified schematic flow diagram of an assembly for removing mercury from crude oil, according to one embodiment.
[0010] Figure 2 is a simplified schematic flow diagram of another assembly for removing mercury from crude oil, according to one embodiment.
[0011] Figure 3 is a graphic illustration of a temperature versus pressure curve, resulting from a simulation, above which temperature 90% mercury removal from a crude oil is predicted. [0012] Figure 4 is a graphic illustration of results from experiments concerning the removal of mercury from decane using methane as a sparging media.
[0013] Figure 5 is a simplified schematic flow diagram of an assembly for removing mercury from crude oil and absorbing hydrocarbon vapors back into the crude oil, according to one embodiment.
[0014] Figure 6 is a graphic illustration of computer simulation results of ratio of mercury in liquid product to mercury in liquid feed versus number of theoretical stages in a gas/liquid contactor used for removing mercury, according to one embodiment.
DETAILED DESCRIPTION OF THE INVENTION
[0015] Embodiments of the invention relate to removal of mercury from crude oil. Such removal relies on transferring mercury from a liquid hydrocarbon stream to a natural gas stream upon contacting the liquid hydrocarbon stream with the natural gas stream. Processing of the natural gas stream after used to strip the mercury from the liquid hydrocarbon stream removes the mercury from the natural gas stream. The removal of the mercury from the crude oil provides marketable products and can be performed onsite at well locations, such as offshore platforms with limited space and facilities, prior to transport to refineries. For example, initial production may contain concentrations of mercury above acceptable thresholds or penalty levels for the refineries such that the removal of the mercury reduces or eliminates penalties and otherwise makes the products marketable.
[0016] Figure 1 illustrates a system in which crude oil is removed from a crude oil well by line 100 and is passed to a separator 102 for separation into a gaseous hydrocarbon stream comprising, consisting of, or consisting essentially of hydrocarbons, mercury and water, which is removed from the separator 102 by line 104, and into a liquid hydrocarbon stream: 1) comprising, consisting of, or consisting essentially of hydrocarbons and elemental mercury, or 2) comprising, consisting of, or consisting essentially of hydrocarbons, elemental mercury and water, which is removed from the separator 102 by line 106. A mercury-containing gas feed, including in part at least a portion of the gaseous hydrocarbon stream, is charged to a mercury removal unit (MRU) 108 by line 110 for removal of mercury from the mercury-containing gas feed, thereby forming a treated gas stream, which is removed from the MRU 108 by line 112. A recycle gas stream comprising a portion of the treated gas stream from the line 112 is charged to a contactor 114 by line 116 for contact with at least a portion of the liquid hydrocarbon stream charged to the contactor 114 by the line 106. Through such contacting, at least a portion of the elemental mercury contained in the liquid hydrocarbon stream is transferred to the recycle gas stream, thereby forming a mercury rich gas stream, which is removed from the contactor 114 by line 118, and a treated liquid hydrocarbon stream, which is removed from the contactor 114 by line 120. The mercury rich gas stream is passed to the MRU 108 as a portion of the mercury- containing gas feed by the lines 118 and 110.
[0017] For some embodiments, the contactor 114 includes multiple (e.g., 2, 4, 6 or more) theoretical stages 122 (depicted by "X" within the contactor 114) of separation between vapor
and liquid phases. Either trays or packing material in a flow path of fluids described herein passing through the contactor 114 may form the theoretical stages 122. For example, the packing material disposed inside of the contactor 114 to define the stages 122 may include random oriented objects or a shaped structure and may be made of metallic or ceramic solid material. In some embodiments, amount of the packing material utilized depends on a desired number of the stages 122 provided by the packing material.
[0018] Figure 2 shows a system in which crude oil is removed from a crude oil well by line 200 and is passed to a first separator 202 for separation into a gaseous hydrocarbon stream comprising, consisting of, or consisting essentially of hydrocarbons, mercury and water, which is removed from the first separator 202 by line 204, and into a liquid hydrocarbon stream comprising, consisting of, or consisting essentially of hydrocarbons, elemental mercury and water, which is removed from the separator 202 by line 206. Along with a mercury rich gas stream described later, the gaseous hydrocarbon stream is charged to a second separator 207 wherein water is removed and exits the second separator 207 by line 208. Overhead gases leaving the second separator 207 by line 209 are charged to a mercury removal unit (MRU) 210 as a mercury-containing gas feed for removal of mercury from the mercury-containing gas feed, thereby forming a treated gas stream, which is removed from the MRU 210 by line 212. A recycle gas stream comprising a portion of the treated gas stream from line 212 is charged to a contactor 214 by line 216 for contact with at least a portion of the liquid hydrocarbon stream charged to the contactor 214 by the line 206. Through such contacting, at least a portion of the elemental mercury contained in the liquid hydrocarbon stream is transferred to the recycle gas stream, thereby forming a mercury rich gas stream, which is removed from the contactor 214 by line 218, and a treated liquid hydrocarbon stream, which is removed from the contactor 214 by line 220. The mercury rich gas stream is passed to the second separator 207 along with the gaseous hydrocarbon stream by the lines 218 and 204. hi addition, water is separated from the liquid hydrocarbon stream (and from the recycle gas stream, if water is present in such) and removed from the contactor 214 by line 222. For some embodiments, a third separator is included in between the first separator 202 and the contactor 214 to separate water from the liquid hydrocarbon stream 206. In some embodiments, a heat exchanger is included after the first separator 202 to increase temperature of the liquid hydrocarbon stream and achieve adequate separation of water from the liquid hydrocarbon stream 206.
[0019] Figure 5 illustrates a system that includes a separator 602, a MRU 608 and a contactor 614, which operate to remove mercury from a crude oil stream as described herein. For some embodiments, another separator is included in between the separator 602 and the contactor 614 to separate water from the liquid hydrocarbon stream. The system further includes a compression and recovery unit 650, a dryer 652, a gas separating unit 654 and a condenser 656 coupled together to facilitate processing associated with removal of the mercury. While only one compressor 651 is shown as part of the recovery unit 650, the compressor 651 may be part of a series of compression, heat exchange and separation within the recovery unit 650 that receives a gaseous hydrocarbon stream 604 from the separator 602 and/or a mercury rich gas stream 618 from the contactor 614. Output from the recovery unit 650 feeds gasses to the MRU 608 and recycles liquids back through the separator 602.
[0020] The dryer 652 removes water vapor from the gasses that pass through the MRU
608, or are introduced into the MRU 608 for embodiments with the dryer located ahead of the MRU 608, prior to the gasses being introduced into the gas separating unit 654. The gas separating unit 654 separates the gasses treated in the MRU 608 into: 1) a propane stream denoted as C3, 2) a butanes stream depicted as C4, 3) a product gas stream 616 that includes methane and ethane (C1-C2), and 4) a pentane-plus gas stream that feeds into the condenser 656 and includes hydrocarbons having at least five carbon atoms per molecule. A portion of the product gas stream 616 enters into a stripping zone 613 of the contactor 614 to achieve the removal of mercury from liquids passing through the contactor 614. In some embodiments, any portion or all of the product gas stream 616 introduced into the stripping zone 613 may bypass separation (i.e., removal of propane, butane and/or pentane-plus) and still achieve mercury and/or propane and butane stripping from the liquids passing through the stripping zone 613 of the contactor 614 as described herein.
[0021] The pentane-plus gas stream introduced into the condenser 656 condenses and is separated into vapors that include pentanes and higher molecular weight hydrocarbons output from the condenser 656 as a blend component stream 657 and liquids (identified as C5+) including hydrocarbons having at least five carbon atoms per molecule. At least a portion of the blend component stream 657 enters into an absorption zone 615 contained in the contactor 614 for transfer of at least a portion of the vapors within the blend component stream 657 to a treated liquid hydrocarbon stream from the stripping zone 613, thereby forming an enriched treated
liquid hydrocarbon stream. The absorption zone 615 provides contact surface area, mixing and residence time sufficient (e.g., via packing material and/or trays shown in figure 5) to absorb at least a portion of the pentanes and higher molecular weight hydrocarbons contained in the blend component stream 657 into the treated liquid hydrocarbon stream. The absorption zone 615 is located in the contactor 614 at a location below the stripping zone 613 such that the treated liquid hydrocarbon stream flows from the stripping zone 613 to the absorption zone 615. The enriched treated liquid hydrocarbon stream provides crude product removed from the contactor 614. [0022] Since propane and butane are stripped from the crude oil stream in the stripping zone 613 of the contactor 614, blending back in contents of the blend component stream 657 in the absorption zone 615 of contactor 614 can occur without exceeding a threshold for vapor pressure in the crude product. Further, utilizing the absorption zone 615 enables limiting amount of the blend component stream 657 that is combined with the mercury rich gas stream 618 entering the recovery unit 650 since the compressor 651 may have limited capacity. Sufficient quantities of the product gas stream 616 can thus pass through the contactor 614 and exit as the mercury rich gas stream 618 to achieve desired reductions in the mercury content within the crude product without overwhelming the capacity of the compressor 651 that receives the mercury rich gas stream 618.
[0023] The crude oil stream in some embodiments comprises, consists of, or consists essentially of a broad range crude oil. For example, the crude oil stream may include hydrocarbons containing at least one carbon atom per molecule. The gaseous hydrocarbon stream comprises, consists of, or consists essentially of hydrocarbons containing from about 1 to about 6 carbon atoms per molecule.
[0024] hi some embodiments, the temperature at which the crude oil stream is separated into the gaseous hydrocarbon stream and the liquid hydrocarbon stream is at least about 50 0C or at least about 60 0C. The pressure at which the crude oil stream is separated into the gaseous hydrocarbon stream and the liquid hydrocarbon stream is at least about 0.5 Bars or at least about 1 Bars, for some embodiments.
[0025] The mercury removal unit has a fixed bed comprising any mercury sorbent material capable of removing mercury from gases, hi some embodiments, the treated gas stream comprises less than about 20 wt. % of the mercury contained in the mercury-containing gas feed or less than about 10 wt. % of the mercury contained in the mercury-containing gas feed. The
treated liquid hydrocarbon stream may comprise less than about 50 wt. % of the elemental mercury contained in the liquid hydrocarbon stream or less than about 20 wt. % of the elemental mercury contained in the liquid hydrocarbon stream. The liquid hydrocarbon stream for some embodiments comprises at least about 10 ppb elemental mercury or comprises at least about 200 ppb elemental mercury.
[0026] The recycle gas stream is contacted with the liquid hydrocarbon stream at a temperature in the range of from about 700C to about 3000C or from about 1500C to about 2000C; a pressure in the range of from about 0.5 Bars to about 15 Bars, from about IBar to about 10
Bars, or from about 2 Bars to about 7 Bars; and a gas to liquid ratio in the range of from about 50 to about 300 standard cubic feet of gas/bbl of liquid (SCF/bbl) or from about 100 to about 200
SCF/bbl.
[0027] The following examples are provided to further illustrate this invention and are not to be considered as limiting the scope of this invention.
EXAMPLES
Example 1
[0028] A simulation of the liquid/gas contactor was constructed using an equation of state thermodynamic prediction model for mercury partitioning between gas and liquid using data for elemental mercury in a naturally obtained crude oil blend. Results of the calculation are shown in Figure 3, wherein the temperature of the crude oil is plotted against the pressure to achieve 90% removal of mercury from the liquid oil feed to the contactor. A gas to oil ratio of
80 SCF/bbl was used in the model.
[0029] Common pressure of a Low Pressure Coalescer/Separator present at the well site
(which is redeployed as set forth herein as a gas/oil contactor) ranges from about < 1 to ~ 3 Bars.
In typical applications, reservoir temperature of high mercury crude oils is greater than about
1500C. This simulation thus shows that 90% mercury removal is achievable at the temperature and pressure conditions often present at the crude oil well site.
Example 2
[0030] An experiment was run to test the removal of elemental mercury (Hg) from a hydrocarbon by sparging with a lighter hydrocarbon. The elemental mercury was dissolved in decane at about 1,300 ppbw. Figure 4 shows the results of the experiment, plotting residual Hg
in the decane versus liters of methane sparged through the decane for two different runs, Runs 1 and 2.
[0031] A third experiment (Run 3) was performed wherein, prior to adding the elemental mercury, the decane was water washed and passed over a silica gel column to remove trace levels of chloride, oxide or sulfur compounds that could, at the conditions of the experiment, oxidize the mercury and cause it to form non-spargable mercury compounds. Also shown in Figure 4 is a plot of the results of theoretical calculations of the mercury removal process. The plot shows that the experimental results for Runs 1 and 2 are in good agreement with the theoretical calculations and that the experimental results for Run 3 are in excellent agreement with the theoretical calculations. Example 3
[0032] A simulation was run in order to evaluate affect of the number of theoretical stages (e.g., as indicated by reference number 122 in figure 1) on mercury removal. Various vapor/liquid (V/L) molar ratios of gas to hydrocarbon liquid were used in the simulations (0.295, 0.147 and 0.074). Results of the model are shown in Figure 6 and demonstrate that for all V/L molar ratios increasing the number of theoretical stages results in increased mercury removal. For instance, increasing the number of theoretical stages from 1 to 5 increased the mercury removal by a factor of four.
[0033] The preferred embodiment of the present invention has been disclosed and illustrated. However, the invention is intended to be as broad as defined in the claims below. Those skilled in the art may be able to study the preferred embodiments and identify other ways to practice the invention that are not exactly as described herein. It is the intent of the inventors that variations and equivalents of the invention are within the scope of the claims below and the description, abstract and drawings are not to be used to limit the scope of the invention.
Claims
1. A process comprising: separating a crude oil stream into a gaseous hydrocarbon stream and a liquid hydrocarbon stream; removing mercury from the gaseous hydrocarbon stream to provide a treated gas stream; contacting the treated gas stream with the liquid hydrocarbon stream to transfer mercury from the liquid hydrocarbon stream to the treated gas stream and thereby form a treated liquid stream and a mercury rich gas stream; and removing mercury from the mercury rich gas stream.
2. The process according to claim 1, wherein contacting the treated gas stream with the liquid hydrocarbon stream includes introducing the treated gas stream and the liquid hydrocarbon stream into a vessel that provides at least two theoretical stages.
3. The process according to claim 2, wherein the vessel includes a packing material in a flow path of the treated gas stream and the liquid hydrocarbon stream.
4. The process according to claim 1, further comprising separating the treated gas stream to form a pentane-plus vapor stream introduced into contact with the treated liquid stream for absorbing into the treated liquid stream.
5. The process according to claim 4, wherein the contacting of the treated gas stream with the liquid hydrocarbon stream further strips propane and butane from the liquid hydrocarbon stream to reduce propane and butane content in the treated liquid stream relative to the liquid hydrocarbon stream.
6. The process according to claim 1, further comprising separating the treated gas stream to remove propane and butane from the treated gas stream prior to contacting the treated gas stream with the liquid hydrocarbon stream.
7. The process according to claim 1, further comprising: separating out a pentane-plus vapor stream from the treated gas stream; and introducing the pentane-plus vapor stream into contact with the treated liquid stream for absorbing into the treated liquid stream, wherein introducing the treated gas stream into contact with the liquid hydrocarbon stream and introducing the pentane-plus vapor stream into contact with the treated liquid stream occur at separate locations.
8. The process according to claim 1, wherein removing mercury from the mercury rich gas stream provides recycled gas providing a portion of the treated gas stream.
9. The process according to claim 1, wherein removing mercury from the gaseous hydrocarbon stream and removing mercury from the mercury rich gas stream comprises introducing the gaseous hydrocarbon stream and the mercury rich gas stream into a mercury-sorbent based removal unit.
10. The process according to claim 1, wherein contacting the treated gas stream with the liquid hydrocarbon stream transfers elemental mercury from the liquid hydrocarbon stream to the treated gas stream.
11. The process according to claim 1, wherein the treated hydrocarbon stream contains less than 10 weight percent of elemental mercury contained in the liquid hydrocarbon stream.
12. A process comprising: transferring mercury from a liquid hydrocarbon stream to a natural gas stream upon contacting the liquid hydrocarbon stream with the natural gas stream and thereby forming a treated liquid stream and a mercury rich gas stream; and removing mercury from the mercury rich gas stream.
13. The process according to claim 12, wherein removing mercury from the mercury rich gas stream provides treated gas forming a portion of the natural gas stream.
14. The process according to claim 12, wherein contacting the liquid hydrocarbon stream with the natural gas stream occurs in a vessel that provides at least two theoretical stages.
15. The process according to claim 12, further comprising: separating a hydrocarbon gas stream into the natural gas stream and a pentane- plus gas stream; and absorbing the pentane-plus gas stream into the treated liquid stream.
16. The process according to claim 12, wherein the natural gas stream has a lower mercury concentration than the liquid hydrocarbon stream prior to contacting the liquid hydrocarbon stream with the natural gas stream.
17. A process comprising: separating a crude oil stream into a gaseous hydrocarbon stream and a liquid hydrocarbon stream; removing mercury from the gaseous hydrocarbon stream to provide a treated gas stream; introducing the treated gas stream into contact with the liquid hydrocarbon stream to transfer mercury from the liquid hydrocarbon stream to the treated gas stream and thereby form a treated liquid stream and a mercury rich gas stream; introducing a pentane-plus vapor stream separated from the treated gas stream into contact with the treated liquid stream for absorbing into the treated liquid stream; and removing mercury from the mercury rich gas stream to provide recycled gas that provides part of the treated gas stream.
18. The process according to claim 17, wherein introducing the treated gas stream into contact with the liquid hydrocarbon stream occurs in a vessel that provides at least two theoretical stages.
19. The process according to claim 17, wherein introducing the treated gas stream into contact with the liquid hydrocarbon stream and introducing the pentane-plus vapor stream into contact with the treated liquid stream occur in separate sections of a contact vessel.
20. The process according to claim 17, wherein the introducing of the treated gas stream into contact with the liquid hydrocarbon stream further strips propane and butane from the liquid hydrocarbon stream to reduce propane and butane content in the treated liquid stream relative to the liquid hydrocarbon stream.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US12/174,816 | 2008-08-11 | ||
US12/174,816 US20100032344A1 (en) | 2008-08-11 | 2008-08-11 | Mercury removal from crude oil |
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WO2010019510A2 true WO2010019510A2 (en) | 2010-02-18 |
WO2010019510A3 WO2010019510A3 (en) | 2010-07-15 |
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PCT/US2009/053292 WO2010019510A2 (en) | 2008-08-11 | 2009-08-10 | Mercury removal from crude oil |
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PCT/US2009/034883 WO2010019282A2 (en) | 2008-08-11 | 2009-02-23 | Mercury removal from crude oil |
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WO (2) | WO2010019282A2 (en) |
Families Citing this family (18)
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US8489231B2 (en) * | 2009-09-18 | 2013-07-16 | Raf Technology, Inc. | Loop mail processing |
US8702975B2 (en) | 2010-09-16 | 2014-04-22 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
US8673133B2 (en) | 2010-09-16 | 2014-03-18 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
US8728304B2 (en) | 2010-09-16 | 2014-05-20 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
US8663460B2 (en) | 2010-09-16 | 2014-03-04 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
US8721874B2 (en) | 2010-11-19 | 2014-05-13 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
US8721873B2 (en) | 2010-11-19 | 2014-05-13 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
US8728303B2 (en) | 2010-11-19 | 2014-05-20 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
EP2508243A1 (en) * | 2011-04-06 | 2012-10-10 | Shell Internationale Research Maatschappij B.V. | Method and apparatus for removing mercury from waste water from hydrocarbon well stream |
WO2013024147A1 (en) | 2011-08-18 | 2013-02-21 | Shell Internationale Research Maatschappij B.V. | System and method for producing a hydrocarbon product stream from a hydrocarbon well stream, and a hydrocarbon well stream separation tank |
CN104093819A (en) * | 2011-12-30 | 2014-10-08 | 雪佛龙美国公司 | Process, method, and system for removing heavy metals from fluids |
SG11201407563QA (en) | 2012-05-16 | 2014-12-30 | Chevron Usa Inc | Process, method, and system for removing mercury from fluids |
US9447674B2 (en) | 2012-05-16 | 2016-09-20 | Chevron U.S.A. Inc. | In-situ method and system for removing heavy metals from produced fluids |
US9023123B2 (en) | 2012-05-16 | 2015-05-05 | Chevron U.S.A. Inc. | Process, method, and system for removing mercury from fluids |
SG11201407510UA (en) | 2012-05-16 | 2014-12-30 | Chevron Usa Inc | Process, method, and system for removing heavy metals from fluids |
US9169445B2 (en) | 2013-03-14 | 2015-10-27 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from oily solids |
US9234141B2 (en) | 2013-03-14 | 2016-01-12 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from oily solids |
US9023196B2 (en) | 2013-03-14 | 2015-05-05 | Chevron U.S.A. Inc. | Process, method, and system for removing heavy metals from fluids |
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US4962276A (en) * | 1989-01-17 | 1990-10-09 | Mobil Oil Corporation | Process for removing mercury from water or hydrocarbon condensate |
US20050167335A1 (en) * | 2004-02-03 | 2005-08-04 | Japan Petroleum Exploration Co., Ltd. | Mercury-removal process in distillation tower |
WO2006090597A1 (en) * | 2005-02-24 | 2006-08-31 | Jgc Corporation | Apparatus for removing mercury in liquid hydrocarbon |
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US3768865A (en) * | 1972-07-13 | 1973-10-30 | Ppg Industries Inc | Process for the disposal of salt solutions contaminated with azide |
JP2578514B2 (en) * | 1989-03-03 | 1997-02-05 | 三井石油化学工業株式会社 | Method for removing mercury from liquid hydrocarbon compounds |
US4983277A (en) * | 1989-04-27 | 1991-01-08 | Mobil Oil Corporation | Process for the production of natural gas condensate having a reduced amount of mercury from a mercury-containing natural gas wellstream |
US4981577A (en) * | 1989-04-27 | 1991-01-01 | Mobil Oil Corporation | Process for the production of natural gas condensate having a reduced amount of mercury from a mercury-containing natural gas wellstream |
US5989506A (en) * | 1996-12-18 | 1999-11-23 | Uop Llc | Process for the removal and recovery of mercury from hydrocarbon streams |
US6350372B1 (en) * | 1999-05-17 | 2002-02-26 | Mobil Oil Corporation | Mercury removal in petroleum crude using H2S/C |
US6537443B1 (en) * | 2000-02-24 | 2003-03-25 | Union Oil Company Of California | Process for removing mercury from liquid hydrocarbons |
US6367555B1 (en) * | 2000-03-15 | 2002-04-09 | Corley P. Senyard, Sr. | Method and apparatus for producing an oil, water, and/or gas well |
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2008
- 2008-08-11 US US12/174,816 patent/US20100032344A1/en not_active Abandoned
-
2009
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- 2009-08-10 WO PCT/US2009/053292 patent/WO2010019510A2/en active Application Filing
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US4962276A (en) * | 1989-01-17 | 1990-10-09 | Mobil Oil Corporation | Process for removing mercury from water or hydrocarbon condensate |
US20050167335A1 (en) * | 2004-02-03 | 2005-08-04 | Japan Petroleum Exploration Co., Ltd. | Mercury-removal process in distillation tower |
WO2006090597A1 (en) * | 2005-02-24 | 2006-08-31 | Jgc Corporation | Apparatus for removing mercury in liquid hydrocarbon |
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US20100032344A1 (en) | 2010-02-11 |
WO2010019510A3 (en) | 2010-07-15 |
WO2010019282A2 (en) | 2010-02-18 |
WO2010019282A3 (en) | 2010-07-15 |
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