CA1302937B - Crude Oil Treater - Google Patents
Crude Oil TreaterInfo
- Publication number
- CA1302937B CA1302937B CA616044A CA616044A CA1302937B CA 1302937 B CA1302937 B CA 1302937B CA 616044 A CA616044 A CA 616044A CA 616044 A CA616044 A CA 616044A CA 1302937 B CA1302937 B CA 1302937B
- Authority
- CA
- Canada
- Prior art keywords
- crude oil
- casing
- liquid
- water
- oil
- 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
Links
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
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Mechanical Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
Heavy crude oil is dehydrated using a conventional treater/ gravity separator, which is connected to a dehydrator into which the crude oil from the treater is distributed to remove residual water. The crude oil is heated in the dehydrator to yield dehydrated heavy hydrocarbons and a mixture of light hydro-carbons. The mixture of light hydrocarbons may be used as a dilu-ent, which may be returned to the treater for diluting the crude oil. Thus, the performance of the pressure treater is substan-tially improved.
Heavy crude oil is dehydrated using a conventional treater/ gravity separator, which is connected to a dehydrator into which the crude oil from the treater is distributed to remove residual water. The crude oil is heated in the dehydrator to yield dehydrated heavy hydrocarbons and a mixture of light hydro-carbons. The mixture of light hydrocarbons may be used as a dilu-ent, which may be returned to the treater for diluting the crude oil. Thus, the performance of the pressure treater is substan-tially improved.
Description
~3V29~7 74304-2X
This invention relates to a method and apparatus for treating crude oil, and in particular heavy hydrocarbon crude oil.
In the treatment of heavy hydrocarbons at or near producing wells, it is desirable to remove all or virtually all of the water entrained in the oil. In general, water can be removed from the oil simply by heating the mixture to boil the water.
However, such boiling, e.g. in a storage tank results in the evolution of steam which creates large quantities of foam formed of steam bubbles in an oil film. The foaming is, at best, diffi-cult to control and forms a spill with a volume many times greaterth`an the volume of the liquid.
Apparatuses for treating crude oil are disclosed, for example by Canadian Patent No. 1,122,135, issued to Koppers Company, Inc. on April 20, 1982, and U.S. Patents Nos. 3,441,499 and 3,453,205, both issued to A. W. Francis, Jr. et al on April 26, 1969 and July 1, 1969, respectively. In general, currently available dehydrators rely on differences in the speci-fic gravity of oil and water to effect gravity separation. The gravity separators use a heat source to raise the temperature of the crude oil which reduces the viscosity of the oil to promote phase separation. Such a process is not particularly effective for heavy crude oils, which have specific gravities close to that of water. The addition of emulsion breakers have often proven to be of little value.
Other dehydrators utilize vacuum towers combined with heaters for removing water as steam below atmospheric pressure.
~3~Z~3~
7430~-2R
The vacuum is created by vapour compressors which condense or flare the resulting pressurized steam to the atmosphere. Such a method requires many separate pieces of equipment, is expensive and is best suited to large central plant facilities. Controlled boiling has also been attempted using tray-type towers or expensive heat exchangers.
An object of the present invention is to provide a relatively simple, easy to operate apparatus which can be located in remote oil producing areas for dehydrating crude oil. Another object of the invention is to provide a method of dehydrating oil which is relatively easy to carry out, even in remote areas.
Accordingly, the present invention relates to a dehydrator for re~oving residual water from heavy crude oil comprising:
(a) a casing;
(b) means defining an inlet for admitting liquid crude oil into the casing so as to establish a liquid surface in the casing;
(c) means defining an outlet passage for discharging dehydrated crude oil from a lower portion of the casing below the liquid surface;
(d) a heater in the casing for maintaining the liquid oil at a distillation temperature for evaporating water and light hydro-carbons;
(e) an outlet duct for discharging a mixture of water vapour and light hydrocarbons evaporated from the crude oil;
(f) distribution means above the surface of the liquid in the casing for distributing incoming crude oil onto and in heat 13~29~
exchange contact with the surface of the heated oil in the casing, whereby water and light hydrocarbon vapours are distilled from incoming crude oll upon contact with the surface of the heated liquid crude oil.
The invention also relates to an apparatus including, in combination with the dehydrator, a treater means for separating a portion of the water and entrained solids from the oil by gravity, and a recycle line for returning at least a portion of the condensed light hydrocarbon fraction for dilution of the crude oil in the treater means, as well as an outlet duct extending from the chamber for directing the vapours from the casing, spray means located in the outlet duct and means for recycling a portion of dehydrated oil from the outlet passage to the spray means for countercurrent spray into the vapours in the outlet duct for suppressing foam on the surface of the liquid in the casing.
The invention also relates to a method for dehydrating crude oil containing water comprising:
(a) providing a casing contalning a quantity of liquid crude oil and having a liquid surface in the casing, and heating the liquid crude oil in the casing for maintaining the liquid crude oil above a distillation temperature;
(b) distributing crude oil containing water onto the surface of the heated liquid crude oil in the casing so as to cause distillation of water and light hydrocarbons from the distributed crude oil;
~3~ 3 7 (c) removing the distilled water and light hydrocarbon vapours from an upper portion of the casing above the liquid surface;
(d) withdrawing dehydrated crude oil from a lower portion of the casing below the liquid surface.
The method may also include a preliminary gravity separation step, recycling of condensed light hydrocarbons, and countercurrent spray of light hydrocarbons, corresponding to the optional additional apparatus elements referred to above.
The combinations of apparatus and process elements claimed as the invention herein are defined in the claims appended hereto, which define the exclusive rights sought by the applicant.
It is preferable that the dehydrated oil has a water content of less than 0.5~ by volume and be acceptable for pipe-line transmission to a refinery. Such oil is readily saleable, particularly in the case of heavy crude oils with specific gravi-ties near or less than that of the produced and accompanying water.
The invention will now be described in greater detail with reference to the accompanying drawings, which illustrate a preferred embodiment of the apparatus of the present invention, and wherein:
Figure 1 is a schematic flow diagram of an apparatus in accordance with the present invention;
- 3a -c_ .
~ 3~2~ ~ 74304-2R
Figure 2 is a schematic longitudinal sectional view of a dehydrator used in the apparatus of Fig. 1 taken generally along line II-II of Fig. 3;
Figure 3 is a cross-section taken along line III-III of Fig. 2; and - Figure 4 is an end view of the dehydrator of Figs. 2 and 3.
With reference to Fig. 1, the apparatus of the present invention includes a treater/gravity separator 1 for receiviny crude oil from an inlet 2 via line 3. The fluid entering the treater 1 is a mixture of oil, water and solid particles such as clays, metals and silicas. The pressure treater 1 is a commercial available item, which operates at pressures from zero to 700 kpa or more, and a temperature of 80 to 140C. The raw crude oil is discharged from the treated 1 through line 4 and valve 5. Such oil contains less water, less oil/water emulsion and less solids, the latter having been separated by gravity and removed with water through a line 6 and a valve 7. Light, unstable hydrocarbon components are discharged from the treater 1 through a vent 8 and a regulating valve 9.
Crude oil from the treater 1 enters a dehydrator gener-ally indicated at 12 which is described hereinafter in greater detail. In the dehydrator 12, oil and water are separated by distillation, water and low boiling temperature hydrocarbon com-ponents of the oil rising through a column 13 and passing through a line 14 to a condenser 15 and then to a vapour/liquid separator 16. Dehydrated oil is discharged from the dehydrator 12 ~.,.
I
through line 17 and a pump 18. Some of the dehydrated oil is returned to the dehydrator 12 through line 19 for stripping additional distillate from the heavy crude oil in column 13.
In the separator 16, water and hydrocarbon distillate are separate by virtue of their different specific gravities. The separated water is discharged through outlet line 20, a pump 21 and a valve 22. A rising liquid level in the separator 16 causes the valve 22 to open, so that the pump 21 discharges the water to storage (not shown). Light, non-condensable components are dis-charged from the separator 16 through vent line 25.
Light hydrocarbon liquid, which has a specific boilingpoint range determined by the operating temperature of dehydrator ~12 and which is stable at atmospheric temperature and pressure is returned to the pressure treater 1 through pipe 26 and line 3, via pump 24. Excess hydrocarbon liquid can be withdrawn -from the system through a line 30 and a valve 31.
Referring to Figs. 2 to 4, the dehydrator 12 of the present invention includes a casing 35 for receiving fluids from the pressure treater 1 through the line 4. The fluid entering the dehydrator 12 flows into a spray tube 36 and is sprayed onto liquid 37 already in the casing 35. In this manner, the liquid being introduced is evenly distributed on the hot crude oil liquid 37 in the dehydrator 12.
The liquid 37 in the dehydrator 12 is heated by a generally U-shaped firetube 40, which is immersed in the liquid.
Fuel is introduced into the tube 40 via inlet end 41 and burned.
Exhaust from the tube 40 is discharged to the atmosphere through a ~ 2~ 74304-2R
vertical discl~arge tube 42.
The liquid 37 is normally at 110 to 150C and a pressure of close to atmospheric, i.e. less than 20 kpa. Boiling occurs at the surface 43 of the liquid 37. The surface 43 acts as a heat sink, liberating water in the form of steam in a direction countercurrent to the incoming crude oil. Virtually all of the water in the crude oil is removed in the dehydrator 12. Light hydrocarbons are liberated with the water, because of the tempera-ture and pressure conditions, and because of steam distillation above the surface 42. Heavy or higher boiling components are stripped from the distillate by dehydrated oil sprayed into the dehydrator 12 through a spray head 45 at the bottom of the column 13. The head 45 receives dehydrated oil from the line 19. The dehydrated oil spray also acts as a foam suppressant by collapsing bubbles 46 at the surface 43 of the liquid 37. The discharge of foam with the distillate is further inhibited by baff:Les 47 extending transversely in the casing 35 on each side of the entrance to the column 13.
In operation, crude oil including oil, water and solids enters the treater 1. In the treater 1, the crude oil is treated to reduce the water, emulsion and solids content of the oil. The crude oil and emulsions flow into the dehydrator 12 where the liquid is evenly distributed on the surface 43 of the oil bath 37.
Water is liberated as steam, and is discharged from the dehydrator 12 with light or low boiling hydrocarbons through the line 14 to the condenser 15. The vapours are converted to liquid water and hydrocarbons which are fed into the separator. In the separator, ~ 3~29~ ~ 74304-2R
the water and hydrocarbons condensate (both low liquid) are separated.
The light hydrocarbon liquid is returned to the treater 1 through the line 26. The liquid is, in effect, a synthetic, tailor-made diluent or solvent, which is readily soluble in the raw crude oil. The composition of the liquid can be altered by controlling the temperature and pressure in the dehydrator 12, and the temperature in the condenser 15. For example, higher tempera-tures and/or lower pressures in the dehydrator 12 will encourage separation of heavier or high boiling point components of the crude oil.
The above described process i5 repeated continuously until the diluent recycled through the line 26 is stabilized, i.e.
of consistently the same composition. As more and more diluent is recycled, the specific gravity of the crude oil in the treater 1 is reduced. For example, a 14 API crude oil is reduced to a 23 API crude oil. Such artificial lowering of the crude oil specific gravity creates a reduction of the overall crude oil viscosity in the pressure treater 1. At selected optimum temperature and pressure, such reduced viscosity encourages the breakup and separation of water/oil emulsions. Water is removed through the valve 7. Solids in the emulsion leave with the water. Initially, the oil flowing into the dehydrator 12 from the treater 1 has a high water content, but as the specific gravity of the oil in the treater 1 decreases, the water content in the line 4 also decreases.
What has been done is to permit the commonly used grav-~3~93 ~ 7430~-2R
ity vessel, namely the pressure treater, to perform the oil and water separation process using an artificial solvent or diluent.
A 3 to 18 API oil is changed to an artificial 18 - 25 API
synthetic crude, which encourages phase separation of oil/water emulsion into separate oil and water steams. This eliminates solids and salt (from salt water) contamination which remains if the crude oil is delivered directly to the evaporative dehydrator Once the synthetic diluent has been created, the pressure treater is as effective as with light conventional crude oils. Any water remaining in the crude oil (usually 0.5 to 1.5~ by volume) can be evaporated in the dehydrator to yield a substantially water-free, low solids crude oil. The process can be expedited if an outside source of diluent is added to the system initially. Once entered and stabilized, the diluent remains in the closed process loop.
In effect, the dehydrator causes upstream conventional equipment to be more effective, so that less energy is required to boil off entrained water.
This invention relates to a method and apparatus for treating crude oil, and in particular heavy hydrocarbon crude oil.
In the treatment of heavy hydrocarbons at or near producing wells, it is desirable to remove all or virtually all of the water entrained in the oil. In general, water can be removed from the oil simply by heating the mixture to boil the water.
However, such boiling, e.g. in a storage tank results in the evolution of steam which creates large quantities of foam formed of steam bubbles in an oil film. The foaming is, at best, diffi-cult to control and forms a spill with a volume many times greaterth`an the volume of the liquid.
Apparatuses for treating crude oil are disclosed, for example by Canadian Patent No. 1,122,135, issued to Koppers Company, Inc. on April 20, 1982, and U.S. Patents Nos. 3,441,499 and 3,453,205, both issued to A. W. Francis, Jr. et al on April 26, 1969 and July 1, 1969, respectively. In general, currently available dehydrators rely on differences in the speci-fic gravity of oil and water to effect gravity separation. The gravity separators use a heat source to raise the temperature of the crude oil which reduces the viscosity of the oil to promote phase separation. Such a process is not particularly effective for heavy crude oils, which have specific gravities close to that of water. The addition of emulsion breakers have often proven to be of little value.
Other dehydrators utilize vacuum towers combined with heaters for removing water as steam below atmospheric pressure.
~3~Z~3~
7430~-2R
The vacuum is created by vapour compressors which condense or flare the resulting pressurized steam to the atmosphere. Such a method requires many separate pieces of equipment, is expensive and is best suited to large central plant facilities. Controlled boiling has also been attempted using tray-type towers or expensive heat exchangers.
An object of the present invention is to provide a relatively simple, easy to operate apparatus which can be located in remote oil producing areas for dehydrating crude oil. Another object of the invention is to provide a method of dehydrating oil which is relatively easy to carry out, even in remote areas.
Accordingly, the present invention relates to a dehydrator for re~oving residual water from heavy crude oil comprising:
(a) a casing;
(b) means defining an inlet for admitting liquid crude oil into the casing so as to establish a liquid surface in the casing;
(c) means defining an outlet passage for discharging dehydrated crude oil from a lower portion of the casing below the liquid surface;
(d) a heater in the casing for maintaining the liquid oil at a distillation temperature for evaporating water and light hydro-carbons;
(e) an outlet duct for discharging a mixture of water vapour and light hydrocarbons evaporated from the crude oil;
(f) distribution means above the surface of the liquid in the casing for distributing incoming crude oil onto and in heat 13~29~
exchange contact with the surface of the heated oil in the casing, whereby water and light hydrocarbon vapours are distilled from incoming crude oll upon contact with the surface of the heated liquid crude oil.
The invention also relates to an apparatus including, in combination with the dehydrator, a treater means for separating a portion of the water and entrained solids from the oil by gravity, and a recycle line for returning at least a portion of the condensed light hydrocarbon fraction for dilution of the crude oil in the treater means, as well as an outlet duct extending from the chamber for directing the vapours from the casing, spray means located in the outlet duct and means for recycling a portion of dehydrated oil from the outlet passage to the spray means for countercurrent spray into the vapours in the outlet duct for suppressing foam on the surface of the liquid in the casing.
The invention also relates to a method for dehydrating crude oil containing water comprising:
(a) providing a casing contalning a quantity of liquid crude oil and having a liquid surface in the casing, and heating the liquid crude oil in the casing for maintaining the liquid crude oil above a distillation temperature;
(b) distributing crude oil containing water onto the surface of the heated liquid crude oil in the casing so as to cause distillation of water and light hydrocarbons from the distributed crude oil;
~3~ 3 7 (c) removing the distilled water and light hydrocarbon vapours from an upper portion of the casing above the liquid surface;
(d) withdrawing dehydrated crude oil from a lower portion of the casing below the liquid surface.
The method may also include a preliminary gravity separation step, recycling of condensed light hydrocarbons, and countercurrent spray of light hydrocarbons, corresponding to the optional additional apparatus elements referred to above.
The combinations of apparatus and process elements claimed as the invention herein are defined in the claims appended hereto, which define the exclusive rights sought by the applicant.
It is preferable that the dehydrated oil has a water content of less than 0.5~ by volume and be acceptable for pipe-line transmission to a refinery. Such oil is readily saleable, particularly in the case of heavy crude oils with specific gravi-ties near or less than that of the produced and accompanying water.
The invention will now be described in greater detail with reference to the accompanying drawings, which illustrate a preferred embodiment of the apparatus of the present invention, and wherein:
Figure 1 is a schematic flow diagram of an apparatus in accordance with the present invention;
- 3a -c_ .
~ 3~2~ ~ 74304-2R
Figure 2 is a schematic longitudinal sectional view of a dehydrator used in the apparatus of Fig. 1 taken generally along line II-II of Fig. 3;
Figure 3 is a cross-section taken along line III-III of Fig. 2; and - Figure 4 is an end view of the dehydrator of Figs. 2 and 3.
With reference to Fig. 1, the apparatus of the present invention includes a treater/gravity separator 1 for receiviny crude oil from an inlet 2 via line 3. The fluid entering the treater 1 is a mixture of oil, water and solid particles such as clays, metals and silicas. The pressure treater 1 is a commercial available item, which operates at pressures from zero to 700 kpa or more, and a temperature of 80 to 140C. The raw crude oil is discharged from the treated 1 through line 4 and valve 5. Such oil contains less water, less oil/water emulsion and less solids, the latter having been separated by gravity and removed with water through a line 6 and a valve 7. Light, unstable hydrocarbon components are discharged from the treater 1 through a vent 8 and a regulating valve 9.
Crude oil from the treater 1 enters a dehydrator gener-ally indicated at 12 which is described hereinafter in greater detail. In the dehydrator 12, oil and water are separated by distillation, water and low boiling temperature hydrocarbon com-ponents of the oil rising through a column 13 and passing through a line 14 to a condenser 15 and then to a vapour/liquid separator 16. Dehydrated oil is discharged from the dehydrator 12 ~.,.
I
through line 17 and a pump 18. Some of the dehydrated oil is returned to the dehydrator 12 through line 19 for stripping additional distillate from the heavy crude oil in column 13.
In the separator 16, water and hydrocarbon distillate are separate by virtue of their different specific gravities. The separated water is discharged through outlet line 20, a pump 21 and a valve 22. A rising liquid level in the separator 16 causes the valve 22 to open, so that the pump 21 discharges the water to storage (not shown). Light, non-condensable components are dis-charged from the separator 16 through vent line 25.
Light hydrocarbon liquid, which has a specific boilingpoint range determined by the operating temperature of dehydrator ~12 and which is stable at atmospheric temperature and pressure is returned to the pressure treater 1 through pipe 26 and line 3, via pump 24. Excess hydrocarbon liquid can be withdrawn -from the system through a line 30 and a valve 31.
Referring to Figs. 2 to 4, the dehydrator 12 of the present invention includes a casing 35 for receiving fluids from the pressure treater 1 through the line 4. The fluid entering the dehydrator 12 flows into a spray tube 36 and is sprayed onto liquid 37 already in the casing 35. In this manner, the liquid being introduced is evenly distributed on the hot crude oil liquid 37 in the dehydrator 12.
The liquid 37 in the dehydrator 12 is heated by a generally U-shaped firetube 40, which is immersed in the liquid.
Fuel is introduced into the tube 40 via inlet end 41 and burned.
Exhaust from the tube 40 is discharged to the atmosphere through a ~ 2~ 74304-2R
vertical discl~arge tube 42.
The liquid 37 is normally at 110 to 150C and a pressure of close to atmospheric, i.e. less than 20 kpa. Boiling occurs at the surface 43 of the liquid 37. The surface 43 acts as a heat sink, liberating water in the form of steam in a direction countercurrent to the incoming crude oil. Virtually all of the water in the crude oil is removed in the dehydrator 12. Light hydrocarbons are liberated with the water, because of the tempera-ture and pressure conditions, and because of steam distillation above the surface 42. Heavy or higher boiling components are stripped from the distillate by dehydrated oil sprayed into the dehydrator 12 through a spray head 45 at the bottom of the column 13. The head 45 receives dehydrated oil from the line 19. The dehydrated oil spray also acts as a foam suppressant by collapsing bubbles 46 at the surface 43 of the liquid 37. The discharge of foam with the distillate is further inhibited by baff:Les 47 extending transversely in the casing 35 on each side of the entrance to the column 13.
In operation, crude oil including oil, water and solids enters the treater 1. In the treater 1, the crude oil is treated to reduce the water, emulsion and solids content of the oil. The crude oil and emulsions flow into the dehydrator 12 where the liquid is evenly distributed on the surface 43 of the oil bath 37.
Water is liberated as steam, and is discharged from the dehydrator 12 with light or low boiling hydrocarbons through the line 14 to the condenser 15. The vapours are converted to liquid water and hydrocarbons which are fed into the separator. In the separator, ~ 3~29~ ~ 74304-2R
the water and hydrocarbons condensate (both low liquid) are separated.
The light hydrocarbon liquid is returned to the treater 1 through the line 26. The liquid is, in effect, a synthetic, tailor-made diluent or solvent, which is readily soluble in the raw crude oil. The composition of the liquid can be altered by controlling the temperature and pressure in the dehydrator 12, and the temperature in the condenser 15. For example, higher tempera-tures and/or lower pressures in the dehydrator 12 will encourage separation of heavier or high boiling point components of the crude oil.
The above described process i5 repeated continuously until the diluent recycled through the line 26 is stabilized, i.e.
of consistently the same composition. As more and more diluent is recycled, the specific gravity of the crude oil in the treater 1 is reduced. For example, a 14 API crude oil is reduced to a 23 API crude oil. Such artificial lowering of the crude oil specific gravity creates a reduction of the overall crude oil viscosity in the pressure treater 1. At selected optimum temperature and pressure, such reduced viscosity encourages the breakup and separation of water/oil emulsions. Water is removed through the valve 7. Solids in the emulsion leave with the water. Initially, the oil flowing into the dehydrator 12 from the treater 1 has a high water content, but as the specific gravity of the oil in the treater 1 decreases, the water content in the line 4 also decreases.
What has been done is to permit the commonly used grav-~3~93 ~ 7430~-2R
ity vessel, namely the pressure treater, to perform the oil and water separation process using an artificial solvent or diluent.
A 3 to 18 API oil is changed to an artificial 18 - 25 API
synthetic crude, which encourages phase separation of oil/water emulsion into separate oil and water steams. This eliminates solids and salt (from salt water) contamination which remains if the crude oil is delivered directly to the evaporative dehydrator Once the synthetic diluent has been created, the pressure treater is as effective as with light conventional crude oils. Any water remaining in the crude oil (usually 0.5 to 1.5~ by volume) can be evaporated in the dehydrator to yield a substantially water-free, low solids crude oil. The process can be expedited if an outside source of diluent is added to the system initially. Once entered and stabilized, the diluent remains in the closed process loop.
In effect, the dehydrator causes upstream conventional equipment to be more effective, so that less energy is required to boil off entrained water.
Claims (32)
1. A method for dehydrating crude oil containing water, comprising providing a casing containing a quantity of liquid crude oil and having a liquid surface in said casing, and heating said liquid crude oil in said casing for maintaining said liquid crude oil above a distillation temperature, spraying crude oil containing water onto the surface of the heating liquid crude oil in the casing so as to cause distillation of water and light hydrocarbons from the sprayed crude oil, removing the distilled water and light hydrocarbon vapors from an upper portion of said casing above said liquid surface, and withdrawing dehydrated crude oil from a lower portion of said casing below said liquid surface.
2. A method as in Claim 1 and including recycling a portion of the withdrawn dehydrated crude oil into said casing.
3. A method as in Claim 1 and including condensing the water and light hydrocarbon vapors removed from said casing and separating the water from said light hydrocarbon vapors by gravity.
4. A method as in Claim 3 and including diluting said crude oil containing water with the condensed, separated light hydro-carbon vapors prior to spraying the crude oil containing water into said casing.
5. A method as in Claim 1 and including subjecting said crude oil containing water to a gravity separation step prior to said spraying step to remove a portion of the water and entrained solids therefrom.
6. A method as in Claim 1 and including maintaining the liquid level in said casing within a predetermined range.
7. A method for dehydrating crude oil containing water, comprising subjecting said crude oil to a gravity separation step to remove a portion of the water and entrained solids therefrom and to produce partially dehydrated crude oil, providing a casing containing a quantity of liquid crude oil heated to a distillation temperature and having a liquid surface in said casing, spraying the partially dehydrated crude oil onto the surface of the heated liquid crude oil so as to cause distillation of water and light hydrocarbons from the sprayed partially dehydrated crude oil, separating the water and light hydrocarbons from the vapor by condensation, spraying a recycled portion of dehydrated crude oil in countercurrent manner to the vapors emanating from said casing, and mixing a recycled portion of the condensed light hydrocarbons with said crude oil prior to said gravity separation step.
8. An apparatus for dehydrating crude oil containing water comprising treater means for separating a portion of said water and entrained solids from the oil by gravity, dehydrator means for receiving the oil containing water remaining in said oil from said treater means, said dehydrator means including a casing for containing said oil and residual water in liquid form in the lower portion thereof so that said liquid has a surface in said casing, and said casing further defining a chamber extending from the upper portion thereof for receiving vapors comprising water and light hydrocarbon fractions emanating from said liquid, and heater means for maintaining the liquid in said casing at an elevated distillation temperature, means for introducing crude oil from said treater means into said casing in the form of a spray from above and onto the surface of said liquid and including means for distributing the spray over the surface of said liquid, a dehydra-ted oil outlet passage for removal of dehydrated oil from said casing, means for separating the residual water from the light hydrocarbon fractions in the condensed vapors, and a recycle line for returning at least a portion of the condensed light hydro-carbon fraction for dilution of said crude oil in said treater means.
9. An apparatus as in Claim 8 and wherein said means for introducing crude oil into said casing comprises an inlet duct; an outlet duct extending from said chamber for directing said vapors from said casing, spray means located in said outlet duct and means for recycling a portion of dehydrated oil from said outlet passage to said spray means for countercurrent spray into the vapors in said outlet duct for suppressing foam on the surface of the liquid in said casing.
10. An apparatus as in Claim 9 and wherein said introducing means includes a spray tube.
11. An apparatus as in Claim 10 and including baffle means positioned in said chamber for preventing the discharge of foam through said outlet duct.
12. An apparatus as in Claim 8 and wherein said heater means includes a substantially U-shaped heater tube positioned within said liquid in -the lower portion of said casing.
13. A dehydrator for removing residual water from heavy crude oil comprising a casing, means defining an inlet for admit-ting liquid crude oil into said casing so as to establish a liquid surface in said casing, means defining an outlet passage for dis-charging dehydrated crude oil from said casing, a heater in said casing for maintaining the liquid oil at a distillation tempera-ture for evaporating water and light hydrocarbons, an outlet duct for discharging a mixture of water vapor and light hydrocarbons distilled from the crude oil, first spray means above said surface of the liquid in said casing for spraying incoming crude oil onto the surface of the heated oil in the casing, and second spray means in said outlet duct and connected to said outlet passage for spraying a recycled portion of dehydrated crude oil into the cas-ing, whereby heavier hydrocarbons contained in the dehydrated crude oil are stripped therefrom by the water and light hydro-carbon vapor mixture.
14. A dehydrator as in Claim 13 and wherein said first spray means comprises a spray tube positioned in a vapor chamber above the surface of the liquid in said casing.
15. A dehydrator as in Claim 14 and including baffle means in said casing for preventing the discharge of foam through said outlet duct.
16. A dehydrator for removing residual water from heavy crude oil comprising a casing, means defining an inlet for admit-ting liquid crude oil into said casing so as to establish a liquid surface in said casing, means defining an outlet passage for dis-charging dehydrated crude oil from said casing, a heater in said casing for maintaining the liquid oil at a distillation tempera-ture for evaporating water and light hydrocarbons, an outlet duct for discharging a mixture of water vapor and light hydrocarbons evaporated from the crude oil, spray means above said surface of the liquid in said casing for spraying incoming crude oil onto and in heat exchange contact with the surface of the heated oil in the casing, whereby water and light hydrocarbon vapors are distilled from incoming crude oil upon contact with the surface of the heated liquid crude oil.
17. A method for dehydrating crude oil containing water, comprising providing a casing containing a quantity of liquid crude oil and having a liquid surface in said casing, and heating said liquid crude oil in said casing for maintaining said liquid crude oil above a distillation temperature, distributing crude oil containing water onto the surface of the heated liquid crude oil in the casing so as to cause distillation of water and light hydrocarbons from the distributed crude oil, removing the distilled water and light hydrocarbon vapors from an upper portion of said casing above said liquid surface, and withdrawing dehydrated crude oil from a lower portion of said casing below said liquid surface.
18. A method as in Claim 17 and including recycling a portion of the withdrawn dehydrated crude oil into said casing.
19. A method as in Claim 17 and including condensing the water and light hydrocarbon vapors removed from said casing and separating the water from said light hydrocarbon vapors by gravity.
20. A method as in Claim 19 and including diluting said crude oil containing water with the condensed, separated light hydrocarbon vapors prior to distributing the crude oil containing water into said casing.
21. A method as in Claim 17 and including subjecting said crude oil containing water to a gravity separation step prior to said distributing step to remove a portion of the water and en-trained solids therefrom.
22. A method as in Claim 17 and including maintaining the liquid level in said casing within a predetermined range.
23. A method for dehydrating crude oil containing water, comprising subjecting said crude oil to a gravity separation step to remove a portion of the water and entrained solids therefrom and to produce partially dehydrated crude oil, providing a casing containing a quantity of liquid crude oil heated to a distillation temperature and having a liquid surface in said casing, distributing the partially dehydrated crude oil onto the surface of the heated liquid crude oil so as to cause distillation of water and light hydrocarbons from the distributed partially dehydrated crude oil, separating the water and light hydrocarbons from the vapor by condensation, spraying a recycled portion of dehydrated crude oil in countercurrent manner to the vapors emanating from said casing, and mixing a recycled portion of the condensed light hydrocarbons with said crude oil prior to said gravity separation step.
24. An apparatus for dehydrating crude oil containing water comprising treater means for separating a portion of said water and entrained solids from the oil by gravity, dehydrator means for receiving the oil containing water remaining in said oil from said treater means, said dehydrator means including a casing for containing said oil and residual water in liquid form in the lower portion thereof so that said liquid has a surface in said casing, and said casing further defining a chamber extending from the upper portion thereof for receiving vapors comprising water and light hydrocarbon fractions emanating from said liquid, and heater means for maintaining the liquid in said casing at an elevated distillation temperature, means for introducing crude oil from said treater means into said casing from above and onto the sur-face of said liquid and including means for distributing the crude oil over the surface of said liquid so as to cause distillation of water and light hydrocarbons from the distributed crude oil, a dehydrated oil outlet passage for removal of dehydrated oil from a lower portion of said casing below said liquid surface, means for separating the residual water from the light hydrocarbon fractions in the condensed vapors, and a recycle line for returning at least a portion of the condensed light hydrocarbon fraction for dilution of said crude oil in said treater means.
25. An apparatus as in Claim 24 and wherein said means for introducing crude oil into said casing comprises an inlet duct;
an outlet duct extending from said chamber for directing said vapors from said casing, spray means located in said outlet duct and means for recycling a portion of dehydrated oil from said outlet passage to said spray means for countercurrent spray into the vapors in said outlet duct for suppressing foam on the surface of the liquid in said casing.
an outlet duct extending from said chamber for directing said vapors from said casing, spray means located in said outlet duct and means for recycling a portion of dehydrated oil from said outlet passage to said spray means for countercurrent spray into the vapors in said outlet duct for suppressing foam on the surface of the liquid in said casing.
26. An apparatus as in Claim 25 and wherein said introducing means includes an apertured tube.
27. An apparatus as in Claim 26 and including baffle means positioned in said chamber for preventing the discharge of foam through said outlet duct.
28. An apparatus as in Claim 24 and wherein said heater means includes a substantially U-shaped heater tube positioned within said liquid in the lower portion of said casing.
29. A dehydrator for removing residual water from heavy crude oil comprising a casing, means defining an inlet for admit-ting liquid crude oil into said casing so as to establish a liquid surface in said casing, means defining an outlet passage for dis-charging dehydrated crude oil from a lower portion of said casing below said liquid surface, a heater in said casing for maintaining the liquid oil at a distillation temperature for evaporating water and light hydrocarbons, an outlet duct for discharging a mixture of water vapor and light hydrocarbons distilled from the crude oil, first distribution means above said surface of the liquid in said casing for distributing incoming crude oil onto the surface of the heated oil in the casing so as to cause distillation of the water and light hydrocarbons from the distributed crude oil, and spray means in said outlet duct and connected to said outlet passage for spraying a recycled portion of dehydrated crude oil into the casing, whereby heavier hydrocarbons contained in the dehydrated crude oil are stripped therefrom by the water and light hydrocarbon vapor mixture.
30. A dehydrator as in Claim 29 and wherein said distribu-tion means comprises an apertured tube positioned in a vapor cham-ber above the surface of the liquid in said casing.
31. A dehydrator as in Claim 30 and including baffle means in said casing for preventing the discharge of foam through said outlet duct.
32. A dehydrator for removing residual water from heavy crude oil comprising a casing, means defining an inlet for admit-ting liquid crude oil into said casing so as to establish a liquid surface in said casing, means defining an outlet passage for dis-charging dehydrated crude oil from a lower portion of said casing below said liquid surface, a heater in said casing for maintaining the liquid oil at a distillation temperature for evaporating water and light hydrocarbons, an outlet duct for discharging a mixture of water vapor and light hydrocarbons evaporated from the crude oil, distribution means above said surface of the liquid in said casing for distributing incoming crude oil onto and in heat ex-change contact with the surface of the heated oil in the casing, whereby water and light hydrocarbon vapors are distilled from incoming crude oil upon contact with the surface of the heated liquid crude oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA616044A CA1302937B (en) | 1991-04-16 | 1991-04-16 | Crude Oil Treater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA616044A CA1302937B (en) | 1991-04-16 | 1991-04-16 | Crude Oil Treater |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1302937B true CA1302937B (en) | 1992-06-09 |
Family
ID=4140936
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA616044A Expired CA1302937B (en) | 1991-04-16 | 1991-04-16 | Crude Oil Treater |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1302937B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6372123B1 (en) | 2000-06-26 | 2002-04-16 | Colt Engineering Corporation | Method of removing water and contaminants from crude oil containing same |
-
1991
- 1991-04-16 CA CA616044A patent/CA1302937B/en not_active Expired
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6372123B1 (en) | 2000-06-26 | 2002-04-16 | Colt Engineering Corporation | Method of removing water and contaminants from crude oil containing same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7097761B2 (en) | Method of removing water and contaminants from crude oil containing same | |
| JPS5818126B2 (en) | Method and apparatus for degassing liquids | |
| KR0133527B1 (en) | Oil recovery process and apparatus for oil refinery waste | |
| US5738762A (en) | Separating oil and water from emulsions containing toxic light ends | |
| US4789461A (en) | Method for removing water from crude oil containing same | |
| US6117275A (en) | Process and device for regenerating a contaminated solvent | |
| US2297297A (en) | Treatment of oil, gas, and water mixtures | |
| CA1296281C (en) | Method of and apparatus for treating waste oil | |
| US20180086987A1 (en) | Dissolved oil removal from quench water of gas cracker ethylene plants | |
| US6042718A (en) | Process for removing water from a water-containing crude oil | |
| US6849175B2 (en) | Method of removing water and contaminants from crude oil containing same | |
| US3057786A (en) | Foam eliminating feed distributor | |
| CA1302937B (en) | Crude Oil Treater | |
| US3043072A (en) | Method and means for treatment of oil well production | |
| CA1257215A (en) | Crude oil treater | |
| USRE33999E (en) | Method of removing water from crude oil containing same | |
| US5328596A (en) | Lubricating oil refining process | |
| CN107880930B (en) | Energy-saving dirty oil dehydration device and treatment method thereof | |
| US5707510A (en) | Crude oil emulsion treating apparatus and method | |
| CA3073593C (en) | Apparatus and method for a remediation plant | |
| US2809923A (en) | Production of catalytic cracking feed stock from petroleum residues by vacuum flashing | |
| US4533366A (en) | Evaporation dehydrator | |
| CN109399888B (en) | Method and device for continuous desalting and dewatering of oily sludge | |
| CA2435344C (en) | Method of removing water and contaminants from crude oil containing same | |
| GB1582015A (en) | Separation by evaporation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| NARE | Reissued | ||
| MKEX | Expiry |