CN108753349B - High-temperature closed dehydration device and method for treating SAGD produced liquid - Google Patents
High-temperature closed dehydration device and method for treating SAGD produced liquid Download PDFInfo
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- CN108753349B CN108753349B CN201810582184.5A CN201810582184A CN108753349B CN 108753349 B CN108753349 B CN 108753349B CN 201810582184 A CN201810582184 A CN 201810582184A CN 108753349 B CN108753349 B CN 108753349B
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- 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
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- 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
- C10G33/04—Dewatering or demulsification of hydrocarbon oils with chemical means
Abstract
The invention relates to the technical field of SAGD produced liquid treatment, in particular to a high-temperature closed dehydration device and a method for treating an SAGD produced liquid. The high-temperature closed dehydration device and the method for treating the SAGD produced liquid are suitable for treating the SAGD produced liquid, realize unpowered operation by using wellhead back pressure, and simultaneously can fully and circularly utilize heat energy and reduce the loss of the heat energy; when the method is used for treating the SAGD produced liquid, compared with the conventional dehydration process, the dehydration time of the method is obviously shortened, the dosage is small, and the oil-crossing index is better; in addition, compared with the foreign dehydration technology, the method can treat the thickened oil with higher difficulty coefficient and has less chemical dosage.
Description
Technical Field
The invention relates to the technical field of SAGD produced liquid treatment, in particular to a high-temperature closed dehydration device and a method for treating an SAGD produced liquid.
Background
Compared with the conventional huff and puff produced liquid, the produced liquid (SAGD produced liquid) has larger differences in basic physical properties, oil-water emulsification characteristics and dehydration mechanism, the conventional dehydration process is difficult to meet the processing requirements of the SAGD produced liquid, foreign companies always implement technical blockade on the technology, and the technology for researching the efficient processing technology of the SAGD produced liquid is a production problem to be solved urgently. The differences in the basic physical properties and dehydration mechanisms of SAGD production fluids and huff and puff development production fluids are mainly manifested in several ways (as shown in table 1).
As can be seen from the table 1, the SAGD produced fluid has the characteristics of high temperature, gas carrying, sand carrying and complex oil-water emulsification type (has obvious colloid characteristics and is in a stable O/W, W/O mixed emulsification state). The SAGD production fluid has dual stability characteristics of colloid and emulsion. The Zeta potential absolute value represents the colloid stability of the produced liquid, and the higher the absolute value is, the stronger the stability is. Through the analysis of a potential method, the Zeta potential absolute values of the SAGD produced liquid are all more than or equal to 40mV and can reach 70mV at most, and are far higher than a huff and puff development area (0 mV to 10 mV), and the SAGD produced liquid has stronger colloid stability, so that the treatment difficulty of the produced liquid is increased. In addition, after the SAGD produced liquid is kept stand for a period of time, the phase separation phenomenon cannot occur, and the microscopic W/O, O/W multiple emulsification state exists through photomicrography; in this state, the conventional oil-water separation process cannot achieve the demulsification effect, and the oil-water separation difficulty is high.
The oil-water separation process commonly used in thickened oil development at present is a two-stage thermochemical large-tank settling dehydration process, most thickened oil treatment stations in Liaohe oil field and Xinjiang oil field adopt the process to treat crude oil, the two-stage thermochemical large-tank settling dehydration process has the problems of long dehydration time, large dosage and the like, the oil exchange index is difficult to meet the dehydration requirement of high-viscosity crude oil, and meanwhile, the open process can bring certain potential safety and environmental protection hazards.
Because the injection and the output of the SAGD development mode are continuous processes, the temperature of produced liquid is as high as 180 ℃ to 200 ℃, and the steam carrying amount is 20 percent to 30 percent, if the open process adopted by the conventional heavy oil treatment is adopted to directly treat the SAGD produced liquid, the heat energy loss is large, and the environmental pollution is serious.
In addition, the treatment temperature of the conventional thick oil treatment process is required to be less than or equal to 100 ℃ due to the open flow, and the temperature is at which the ultra-thick oil (50 ℃, 5 multiplied by 10) is treated4mPa.s to 20X 104mpa.s) viscosity is still at a high level (2000 to 10000 mpa.s), and the crude oil has poor fluidity in this state, so that high-efficiency separation of oil and water is difficult to realize.
Disclosure of Invention
The invention provides a high-temperature closed dehydration device and a method for treating SAGD produced liquid, overcomes the defects of the prior art, and can effectively solve the problems that the conventional oil-water separation process is not suitable for treating the SAGD produced liquid, and the conventional oil-water separation process has long dehydration time, large dosage and poor oil-mixing index.
One of the technical schemes of the invention is realized by the following measures: a high-temperature closed dehydration device comprises a high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device, a super-thick oil high-temperature high-efficiency elevation-angle type pre-dehydration device, a dehydrator, a pressure oil remover, a first heat exchanger, a second heat exchanger, a third heat exchanger and a fourth heat exchanger, wherein an inlet of the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device is communicated with a produced liquid inlet pipe, a liquid outlet of the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device is communicated with an inlet of a heat source channel of the first heat exchanger, a gas outlet of the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device is communicated with an inlet of the heat source channel of the second heat exchanger, an outlet of the heat source channel of the second heat exchanger is communicated with a condensed water pipe, an outlet of the heat source channel of the first heat exchanger is communicated with an inlet of the super-thick oil high-temperature high-efficiency elevation-angle, an oil outlet of the dehydrator is communicated with a heat source channel inlet of the third heat exchanger, a heat source channel outlet of the third heat exchanger is communicated with a purified oil pipe, a water outlet of the ultra-thick oil high-temperature high-efficiency elevation-type pre-dehydration device is communicated with an inlet of the pressure oil remover, a water outlet of the dehydrator is communicated with an inlet of the pressure oil remover, a water outlet of the pressure oil remover is communicated with a heat source channel inlet of the fourth heat exchanger, and a heat source channel outlet of the fourth heat exchanger is communicated with a condensate pipe; a cold source channel inlet of the first heat exchanger, a cold source channel inlet of the second heat exchanger, a cold source channel inlet of the third heat exchanger and a cold source channel inlet of the fourth heat exchanger are communicated through pipelines; the cold source channel outlet of the first heat exchanger, the cold source channel outlet of the second heat exchanger, the cold source channel outlet of the third heat exchanger and the cold source channel outlet of the fourth heat exchanger are communicated through pipelines.
The following is a further optimization or/and improvement of one of the above-mentioned technical solutions of the invention:
the high-temperature closed dehydration device also comprises a heat energy centralized utilization unit, an ethylene glycol buffer tank and an ethylene glycol circulating pump; the cold source channel outlet of the first heat exchanger, the cold source channel outlet of the second heat exchanger, the cold source channel outlet of the third heat exchanger and the cold source channel outlet of the fourth heat exchanger are respectively communicated with the inlet of the heat energy centralized utilization unit through pipelines, the outlet of the heat energy centralized utilization unit is communicated with the inlet of the ethylene glycol buffer tank, the outlet of the ethylene glycol buffer tank is communicated with the inlet of the ethylene glycol circulating pump, the cold source channel inlet of the first heat exchanger, the cold source channel inlet of the second heat exchanger, the cold source channel inlet of the third heat exchanger and the cold source channel inlet of the fourth heat exchanger are respectively communicated with the outlet of the ethylene glycol circulating pump through pipelines.
The dehydrator is a thermoelectric chemical combined dehydration device or a high-temperature thermochemical dehydrator of the super heavy oil or an electric dehydrator of the super heavy oil high-temperature crude oil; or/and the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger all adopt ethylene glycol heat exchangers; or/and the high-temperature gas-carrying super-heavy oil slug flow trapping and processing integrated device is provided with a gas port capable of supplementing gas and relieving pressure.
The second technical scheme of the invention is realized by the following measures: a method for treating SAGD produced liquid by adopting the high-temperature closed dehydration device in one of the technical schemes is carried out according to the following method: gas-liquid separation is carried out on the SAGD produced liquid with the temperature of 165-177 ℃ through a high-temperature steam-carrying super-thick oil slug flow trapping treatment integrated device to obtain degassed produced liquid and a gas phase containing steam and associated gas; the gas phase containing the steam and the associated gas is subjected to heat exchange and temperature reduction through a second heat exchanger; the method comprises the following steps that (1) after the degassed produced liquid is subjected to heat exchange and temperature reduction through a first heat exchanger, the temperature of the degassed produced liquid is kept in a supercooled state, the degassed produced liquid in the supercooled state enters an ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device for gel breaking treatment to obtain a water-containing oil phase and an oil-containing water phase, the water-containing oil phase enters a dehydrator for emulsion breaking and dehydration treatment to obtain purified oil and produced water, and the produced water and the oil-containing water phase enter a pressure oil remover for oil removal treatment to obtain oil; and the purified oil exchanges heat with the third heat exchanger for cooling, and the oil-removed produced water exchanges heat with the fourth heat exchanger for cooling.
The following is further optimization or/and improvement of the second technical scheme of the invention:
after the gas phase containing the steam and the associated gas is subjected to heat exchange through a second heat exchanger, the temperature of the gas phase is reduced from 165 ℃ to 177 ℃ to 85 ℃ to 90 ℃; or/and the temperature of the degassed produced fluid after heat exchange and temperature reduction by the first heat exchanger is kept in a state of supercooling from 20 ℃ to 22 ℃.
And when the degassed produced liquid in the supercooled state enters the high-temperature high-efficiency elevation type pre-dehydration device for gel breaking treatment, adding a gel breaker into the high-temperature high-efficiency elevation type pre-dehydration device for the super-thick oil, wherein the addition amount of the gel breaker is 80mg/L to 85 mg/L.
The gel breaker adopts polyether gel breaker.
When the water-containing oil phase enters a dehydrator for demulsification and dehydration treatment, a demulsifier is added into the dehydrator, and the dosage of the demulsifier is 100mg/L to 150 mg/L.
The demulsifier adopts polyester demulsifier.
The cold sources in the cold source channels of the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger are all ethylene glycol, the ethylene glycol subjected to heat exchange and temperature rise enters the heat energy centralized utilization unit to be subjected to heat energy recycling, and the ethylene glycol subjected to heat energy recycling is reused as the cold sources in the cold source channels of the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger to be recycled.
The high-temperature closed dehydration device and the method for treating the SAGD produced liquid are suitable for treating the SAGD produced liquid, realize unpowered operation by using wellhead back pressure, and simultaneously can fully and circularly utilize heat energy and reduce the loss of the heat energy; when the method is used for treating the SAGD produced liquid, compared with the conventional dehydration process (two-stage large tank open process), the method has the advantages of obviously shortened dehydration time, small dosage and better oil-crossing index; in addition, compared with the foreign dehydration technology, the method can treat the thickened oil with higher difficulty coefficient, the dosage is less, the treated oil-crossing index is in the same level and reaches the international advanced level, and thus the technical bottleneck of SAGD produced liquid treatment is broken through.
Drawings
FIG. 1 is a process flow diagram of example 1 of the present invention.
In the drawings: 1 is high temperature and carries vapour super viscous crude section plug flow entrapment processing integrated device, 2 is super viscous crude high temperature high efficiency elevation angle formula dehydration device in advance, 3 is the dehydrator, 4 is the pressure degreaser, 5 is first heat exchanger, 6 is the second heat exchanger, 7 is the third heat exchanger, 8 is the fourth heat exchanger, 9 is the extraction liquid feed liquor pipe, 10 is the condensate pipe, 11 is oil purification pipe, 12 is the unit of utilizing in heat energy concentration, 13 is the ethylene glycol buffer tank, 14 is the ethylene glycol circulating pump.
Detailed Description
The present invention is not limited by the following examples, and specific embodiments may be determined according to the technical solutions and practical situations of the present invention. The various devices, chemical reagents and chemical articles mentioned in the present invention are all the devices, chemical reagents and chemical articles which are well known and commonly used in the prior art, unless otherwise specified; the percentages in the present invention are all mass percentages unless otherwise specified.
The invention is further described below with reference to the following examples:
example 1: as shown in attached figure 1, the high-temperature closed dehydration device comprises a high-temperature vapor-carrying super-thick oil slug flow trapping and processing integrated device 1, a super-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2, a dehydrator 3, a pressure oil remover 4, a first heat exchanger 5, a second heat exchanger 6, a third heat exchanger 7 and a fourth heat exchanger 8, wherein an inlet of the high-temperature vapor-carrying super-thick oil slug flow trapping and processing integrated device 1 is communicated with a produced liquid inlet pipe 9, a liquid outlet of the high-temperature vapor-carrying super-thick oil slug flow trapping and processing integrated device 1 is communicated with a heat source channel inlet of the first heat exchanger 5, a gas outlet of the high-temperature vapor-carrying super-thick oil slug flow trapping and processing integrated device 1 is communicated with a heat source channel inlet of the second heat exchanger 6, a heat source channel outlet of the second heat exchanger 6 is communicated with a condensed water pipe 10, a heat source channel outlet of the first heat exchanger 5 is communicated with an inlet of the super, an oil outlet of the ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 is communicated with an oil inlet of a dehydrator 3, an oil outlet of the dehydrator 3 is communicated with a heat source channel inlet of a third heat exchanger 7, a heat source channel outlet of the third heat exchanger 7 is communicated with a purification oil pipe 11, a water outlet of the ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 is communicated with an inlet of a pressure oil remover 4, a water outlet of the dehydrator 3 is communicated with an inlet of the pressure oil remover 4, a water outlet of the pressure oil remover 4 is communicated with a heat source channel inlet of a fourth heat exchanger 8, and a heat source channel outlet of the fourth heat exchanger 8 is communicated with a condensate; a cold source channel inlet of the first heat exchanger 5, a cold source channel inlet of the second heat exchanger 6, a cold source channel inlet of the third heat exchanger 7 and a cold source channel inlet of the fourth heat exchanger 8 are communicated through pipelines; the cold source channel outlet of the first heat exchanger 5, the cold source channel outlet of the second heat exchanger 6, the cold source channel outlet of the third heat exchanger 7 and the cold source channel outlet of the fourth heat exchanger 8 are communicated through pipelines.
The integrated device 1 for high-temperature entrained-steam super-heavy oil slug flow trapping treatment is a Chinese patent application document with the application number of 201520354953.8.
The super heavy oil high-temperature high-efficiency elevation-type pre-dehydration device 2 is a Chinese patent application document with the application number of 201310569350.5.
Aiming at the characteristics of complex high-temperature, steam carrying, sand carrying and oil-water emulsification types of the SAGD produced liquid, the high-temperature closed dehydration device is combined with a high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device 1, a super-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2, a dehydrator 3 and a pressure oil remover 4 to process the SAGD produced liquid, the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device 1 is used for carrying out gas (steam) liquid separation on the SAGD produced liquid, then a first heat exchanger 5 is used for carrying out heat exchange and temperature reduction, the degassed produced liquid obtained after gas-liquid separation is firstly subjected to gel breaking and destabilization in the super-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2, electric neutralization and gel breaking are carried out, oil drops are rapidly separated and aggregated from water to form a continuous phase, the oil-water preliminary separation is realized, and then the preliminarily separated low-water-containing crude oil (, the stabilization effect of asphaltene, colloid and the like in the emulsion is destroyed, the surface activity of the clay particles of the silt is reduced, so that water drops of the inner phase (oil phase) are discharged from the cage breaking mode, tiny water drops discharged from the cage breaking mode are subjected to violent Brownian motion collision at high temperature, are coalesced into large water drops and are finally settled, and the oil-water separation is better realized; in addition, the device recycles heat energy through the first heat exchanger 5, the second heat exchanger 6, the third heat exchanger 7 and the fourth heat exchanger 8.
The first heat exchanger 5 functions in the device of the invention: the produced liquid after gas (vapor) liquid separation is high-temperature saturated fluid, the friction of a rear-end pipeline and a system is inevitable, the saturated liquid can be subjected to local flash evaporation along with the pressure change, the rear-end oil-water separation environment is unstable, the dehydration effect is further influenced, after heat exchange is carried out through the first heat exchanger 5, the supercooling degree of the degassed produced liquid is ensured to be 10-22 ℃, even if pressure fluctuation occurs in a rear-end system, flash evaporation cannot occur in the supercooled liquid, the stability of the oil-water separation environment can be guaranteed, and the dehydration effect is greatly improved.
The device is more suitable for oil-water separation of the SAGD produced liquid.
The following are further optimization or/and improvement on the high-temperature closed dehydration device:
as shown in the attached figure 1, the high-temperature closed dehydration device further comprises a heat energy centralized utilization unit 12, an ethylene glycol buffer tank 13 and an ethylene glycol circulating pump 14; the cold source channel outlet of the first heat exchanger 5, the cold source channel outlet of the second heat exchanger 6, the cold source channel outlet of the third heat exchanger 7 and the cold source channel outlet of the fourth heat exchanger 8 are respectively communicated with the inlet of the heat energy centralized utilization unit 12 through pipelines, the outlet of the heat energy centralized utilization unit 12 is communicated with the inlet of the ethylene glycol buffer tank 13, the outlet of the ethylene glycol buffer tank 13 is communicated with the inlet of the ethylene glycol circulating pump 14, the cold source channel inlet of the first heat exchanger 5, the cold source channel inlet of the second heat exchanger 6, the cold source channel inlet of the third heat exchanger 7 and the cold source channel inlet of the fourth heat exchanger 8 are respectively communicated with the outlet of the pipeline ethylene glycol circulating pump 14.
The recovered heat energy is used by the heat energy concentrated utilization unit 12: the high-grade heat source can be used for boiler feed water heat exchange, multi-effect evaporation and the like, the medium-grade heat source is used for station heating and heat tracing, and the low-grade waste heat is used for air cooling and environment-friendly disposal.
According to the requirement, the dehydrator 3 is a thermoelectric chemical combined dehydration device or a high-temperature thermochemical dehydrator of the super heavy oil or an electric dehydrator of the super heavy oil high-temperature crude oil; or/and the first heat exchanger 5, the second heat exchanger 6, the third heat exchanger 7 and the fourth heat exchanger 8 all adopt ethylene glycol heat exchangers; or/and the high-temperature gas-carrying super-heavy oil slug flow trapping and processing integrated device 1 is provided with a gas port capable of supplementing gas and relieving pressure.
The use of the combined heat and power dehydration device or the high-temperature thermochemical dehydrator of the super heavy oil or the high-temperature crude oil electric dehydrator of the super heavy oil can further improve the dehydration effect, thereby improving the recovery rate of the crude oil.
The ethylene glycol heat exchanger adopts a heat exchanger with a heat exchange medium of ethylene glycol.
The combined heat and power chemical dehydration device is the Chinese patent application with the application number of 201520354922.2.
Chinese patent application document 201320721197.9 discloses a high-temperature thermochemical dehydrator for super heavy oil 3.
The super heavy oil high temperature crude oil electric dehydrator 3 is 201320721238.4.
Because the SAGD produced liquid is pressurized, the device of the invention fully utilizes wellhead back pressure (generally 1.0MPa to 1.6 MPa), and the whole process realizes high-temperature unpowered operation. When the back pressure of the well mouth is insufficient, natural gas is supplemented through the gas port, so that the pressure meets the operation requirement; when the back pressure of the wellhead is too high, partial pressure can be discharged through the air port, and the safe operation of the device is ensured.
The combination of the primary heat exchange (the first heat exchanger 5) and the air supply and pressure relief process can always ensure that the fluid runs at the supercooled state of 15-22 ℃, and the influence of flash evaporation on the treatment process is eliminated.
Example 2: the method for treating the SAGD produced liquid by adopting the high-temperature closed dehydration device in the embodiment 1 is carried out according to the following method: gas-liquid separation is carried out on SAGD produced liquid with the temperature of 165-177 ℃ through a high-temperature steam-carrying super-thick oil slug flow trapping treatment integrated device 1 to obtain degassed produced liquid and a gas phase containing steam and associated gas; the gas phase containing the steam and the associated gas is subjected to heat exchange and temperature reduction through a second heat exchanger 6; the method comprises the following steps that (1) after the degassed produced liquid is subjected to heat exchange and temperature reduction through a first heat exchanger 5, the temperature of the degassed produced liquid is kept in a supercooled state, the degassed produced liquid in the supercooled state enters an ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 for gel breaking treatment to obtain a water-containing oil phase and an oil-containing water phase, the water-containing oil phase enters a dehydrator 3 for demulsification and dehydration treatment to obtain purified oil and produced water, and the produced water and the oil-containing water phase enter a pressure oil remover 4 for oil removal treatment to obtain deoil; the purified oil exchanges heat with the third heat exchanger 7 to reduce the temperature, and the oil-removed produced water exchanges heat with the fourth heat exchanger 8 to reduce the temperature.
In the method for treating the SAGD produced liquid, the whole process is continuously carried out in a closed state, so that the process is a high-temperature closed dehydration process, the SAGD produced liquid is subjected to gas (steam) liquid separation through a high-temperature steam-carrying super-thick oil section plug flow trapping treatment integrated device 1, heat exchange and temperature reduction are carried out through a first heat exchanger 5, degassed produced liquid obtained after gas-liquid separation is subjected to gel breaking and destabilization firstly in a super-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2, electric neutralization and gel breaking are carried out, oil drops are rapidly separated and aggregated from water to form a continuous phase, oil-water primary separation is realized, then low-water-content crude oil (water-containing oil phase) which is primarily separated is subjected to emulsion breaking and dehydration in a dehydrator 3, the stabilizing action of asphaltene, colloid and the like in emulsion is destroyed, the surface activity of silt clay particles is reduced, and water drops of an inner phase (oil phase) are led to be broken into cages, the tiny water drops which are produced by cage breaking do violent Brownian motion collision at high temperature, coalesce into large-particle water drops, and finally settle down, thereby better realizing the separation of oil and water.
The method for treating the SAGD produced liquid fully utilizes wellhead back pressure, and high-temperature unpowered operation is achieved.
When the SAGD produced fluid is treated by the method, the SAGD produced fluid is compared with the conventional dehydration process, and the comparison result is shown in the table 2.
As can be seen from Table 2, the method of the embodiment has the advantages of obviously shortened dehydration time, small dosage, better oil blending index and lower water content of the oil blending.
Example 3: the method for treating the SAGD produced liquid by adopting the high-temperature closed dehydration device in the embodiment 1 is carried out according to the following method: gas-liquid separation is carried out on SAGD produced liquid at the temperature of 165 ℃ or 177 ℃ through a high-temperature steam-carrying super-thick oil slug flow trapping treatment integrated device 1 to obtain degassed produced liquid and a gas phase containing steam and associated gas; the gas phase containing the steam and the associated gas is subjected to heat exchange and temperature reduction through a second heat exchanger 6; the method comprises the following steps that (1) after the degassed produced liquid is subjected to heat exchange and temperature reduction through a first heat exchanger 5, the temperature of the degassed produced liquid is kept in a supercooled state, the degassed produced liquid in the supercooled state enters an ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 for gel breaking treatment to obtain a water-containing oil phase and an oil-containing water phase, the water-containing oil phase enters a dehydrator 3 for demulsification and dehydration treatment to obtain purified oil and produced water, and the produced water and the oil-containing water phase enter a pressure oil remover 4 for oil removal treatment to obtain deoil; the purified oil exchanges heat with the third heat exchanger 7 to reduce the temperature, and the oil-removed produced water exchanges heat with the fourth heat exchanger 8 to reduce the temperature.
The method of example 3, which also has the same treatment effect on SAGD production fluids as example 2.
Example 4: as optimization of the above embodiment, the temperature of the gas phase containing steam and associated gas is reduced from 165 ℃ to 177 ℃ to 85 ℃ to 90 ℃ after heat exchange by the second heat exchanger 6; or/and the temperature of the degassed produced fluid after heat exchange and temperature reduction by the first heat exchanger 5 is kept in a state of supercooling from 20 ℃ to 22 ℃.
Example 5: as optimization of the embodiment, when the degassed produced fluid in the supercooled state enters the high-temperature high-efficiency elevation type pre-dehydration device 2 for gel breaking treatment, a gel breaker is added into the high-temperature high-efficiency elevation type pre-dehydration device 2 for the super-thick oil, and the addition amount of the gel breaker is 80mg/L to 85 mg/L.
The silt in the produced liquid is subjected to solid-liquid separation under the action of the gel breaker and is discharged through the ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2, so that the possibility that the muddy components become an emulsifier is eliminated, and the demulsification and dehydration efficiency of the dehydrator 3 is improved.
Example 6: as the optimization of example 5, a polyether breaker was used as the breaker.
Polyether breakers are a class of breakers in the prior art. The polyether gel breaker can further improve the gel breaking effect.
Example 7: as the optimization of the embodiment, when the aqueous oil phase enters the dehydrator 3 for demulsification and dehydration treatment, the demulsifier is added into the dehydrator 3, and the dosage of the demulsifier is 100mg/L to 150 mg/L.
Example 8: as the optimization of the above example 7, the demulsifier used was a polyester-based demulsifier.
Polyester demulsifiers are a class of demulsifiers known in the art. The polyester demulsifier can further improve the demulsification effect.
Example 9: as optimization of the above embodiment, the cold sources in the cold source channels of the first heat exchanger 5, the second heat exchanger 6, the third heat exchanger 7 and the fourth heat exchanger 8 all use ethylene glycol, the ethylene glycol after heat exchange and temperature rise enters the heat energy centralized utilization unit 12 for heat energy recycling, and the ethylene glycol after heat energy recycling is used as the cold source in the cold source channels of the first heat exchanger 5, the second heat exchanger 6, the third heat exchanger 7 and the fourth heat exchanger 8 for recycling. Thereby utilizing the heat energy of the SAGD produced liquid to the maximum extent.
Example 10: the method for treating the SAGD produced liquid comprises the following steps: liquid (SAGD produced liquid) from an oil area enters a high-temperature steam-carrying super-thick oil slug flow trapping treatment integrated device 1 to be subjected to gas (steam) liquid separation, the separated steam and associated gas are sent to a second heat exchanger 6 to be subjected to heat exchange (the temperature is reduced from 177 ℃ to 90 ℃), and condensed water after the heat exchange is sent to a water treatment system;
the degassed produced fluid obtained after gas (vapor) liquid separation enters a first heat exchanger 5 for heat exchange (the temperature is reduced from 177 ℃ to 155 ℃), enters an ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 for gel breaking and destabilization in a supercooling 20 ℃ state, the produced fluid with low water content (10-20%) separated from the ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 enters a thermoelectrochemistry combined dehydration device for crude oil dehydration, the dehydrated purified oil enters a third heat exchanger 7 for heat exchange (the temperature is reduced from 140 ℃ to 95 ℃), and the purified oil after heat exchange enters an external transportation system;
the produced water separated by the ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device 2 and the thermoelectrochemistry combined dehydration device enters a fourth heat exchanger 8 for heat exchange (the temperature is reduced from 150 ℃ to 95 ℃) after being deoiled by a pressure oil remover 4, and the produced water after heat exchange is subjected to a water removal treatment system.
Example 11: the method for treating the SAGD produced liquid in the embodiment is popularized and applied to engineering of high-temperature closed dehydration test stations for SAGD produced liquid in wind cities. The station is designed to be 30 x 10 in size4t/a, putting into production in 12 months in 2012, and at present, cumulatively treating 1260 ten thousand tons of SAGD produced liquid and 189 ten thousand tons of crude oil to reach the indexes that the water content of the cross oil is less than or equal to 0.5 percent and the oil content of the produced water is less than or equal to 300mg/L under the condition that the dosage of various medicaments is less than or equal to 250 mg/L.
The standard alignment of the method for treating the SAGD produced liquid and the SAGD development oil field treatment process at home and abroad is shown in Table 3.
As can be seen from Table 3, compared with the domestic conventional thickened oil dehydration technology, the treatment level of the method for treating the SAGD produced liquid reaches the domestic leading level; compared with the foreign dehydration technology, the crude oil treatment is more than 6 times of the viscosity of the foreign oil field, the dosage is less, the oil exchange index after the treatment is at the same level, the treatment difficulty coefficient is far higher than that of the foreign oil field, and the whole process technology reaches the international advanced level.
In conclusion, the high-temperature closed dehydration device and the method for treating the SAGD produced liquid are suitable for treating the SAGD produced liquid, unpowered operation is realized by using wellhead back pressure, heat energy can be fully recycled, and loss of the heat energy is reduced; when the method is used for treating the SAGD produced liquid, compared with the conventional dehydration process (two-stage large tank open process), the method has the advantages of obviously shortened dehydration time, small dosage and better oil-crossing index; in addition, compared with the foreign dehydration technology, the method can treat the thickened oil with higher difficulty coefficient, the dosage is less, the treated oil-crossing index is in the same level and reaches the international advanced level, and thus the technical bottleneck of SAGD produced liquid treatment is broken through.
The technical characteristics form an embodiment of the invention, which has strong adaptability and implementation effect, and unnecessary technical characteristics can be increased or decreased according to actual needs to meet the requirements of different situations.
Claims (11)
1. A high-temperature closed dehydration device is characterized by comprising a high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device, a super-thick oil high-temperature high-efficiency elevation type pre-dehydration device, a dehydrator, a pressure oil remover, a first heat exchanger, a second heat exchanger, a third heat exchanger and a fourth heat exchanger, wherein an inlet of the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device is communicated with a produced liquid inlet pipe, a liquid outlet of the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device is communicated with a heat source channel inlet of the first heat exchanger, a gas outlet of the high-temperature steam carrying super-thick oil section plug flow trapping and processing integrated device is communicated with a heat source channel inlet of the second heat exchanger, a heat source channel outlet of the second heat exchanger is communicated with a condensed water pipe, a heat source channel outlet of the first heat exchanger is communicated with an inlet of the super-thick oil high-temperature high-efficiency elevation type pre-dehydration device, an oil outlet of the super, an oil outlet of the dehydrator is communicated with a heat source channel inlet of the third heat exchanger, a heat source channel outlet of the third heat exchanger is communicated with a purified oil pipe, a water outlet of the ultra-thick oil high-temperature high-efficiency elevation-type pre-dehydration device is communicated with an inlet of the pressure oil remover, a water outlet of the dehydrator is communicated with an inlet of the pressure oil remover, a water outlet of the pressure oil remover is communicated with a heat source channel inlet of the fourth heat exchanger, and a heat source channel outlet of the fourth heat exchanger is communicated with a condensate pipe; a cold source channel inlet of the first heat exchanger, a cold source channel inlet of the second heat exchanger, a cold source channel inlet of the third heat exchanger and a cold source channel inlet of the fourth heat exchanger are communicated through pipelines; a cold source channel outlet of the first heat exchanger, a cold source channel outlet of the second heat exchanger, a cold source channel outlet of the third heat exchanger and a cold source channel outlet of the fourth heat exchanger are communicated through pipelines; wherein the content of the first and second substances,
the high-temperature steam-carrying super-heavy oil slug flow trapping and treating integrated device comprises a steam processor, a prying seat and a slug flow trap; the steam processor is fixedly arranged on the prying seat through a support, a liquid inlet end is arranged at the lower part of the left end of the steam processor, a liquid outlet end is arranged in the middle of the right end of the steam processor, a liquid outlet pipe is fixedly arranged on the liquid outlet end, and a rotational flow liquid remover is fixedly arranged at the top end of the left part of the steam processor; the segmented plug flow catcher is provided with a liquid outlet end and a vapor outlet end, the liquid outlet end of the segmented plug flow catcher and the liquid inlet end of the steam processor are fixedly connected together through a liquid phase connecting pipe, the lower part of the cyclone liquid remover is provided with a vapor inlet end along the tangential direction, the vapor outlet end of the segmented plug flow catcher and the vapor inlet end of the cyclone liquid remover are fixedly connected together through a vapor phase connecting pipe, the top of the cyclone liquid remover is fixedly connected with a first gas outlet pipe, the top end of the right part of the steam processor is fixedly connected with a second gas outlet pipe, and the first gas outlet pipe and the second gas outlet pipe are fixedly communicated together; a liquid discharge valve is fixedly arranged on a liquid outlet pipe of the steam processor, and an exhaust valve is fixedly arranged on a first air outlet pipe;
the high-temperature high-efficiency elevation angle type pre-dehydration device for the ultra-thick oil comprises a tank body, an oil outlet collector, a water removal coalescer, an oil removal coalescer and a sand washing device, wherein the tank body is in a left-low-right high-inclination shape, and the included angle between the tank body and a horizontal plane is 9-15 degrees; an oil outlet collector is fixed in the right part of the tank body, and a liquid inlet cavity is formed between the oil outlet collector and the right end of the tank body; a liquid inlet port is arranged on the tank body at the upper part of the liquid inlet cavity; a dewatering coalescer is fixedly arranged in the tank body on the left side of the oil outlet collector, and a collecting tank is formed between the dewatering coalescer and the oil outlet collector; an oil inlet port and an oil outlet port are formed in the oil outlet collector, the oil inlet port is communicated with the collecting tank, and the oil outlet port is communicated with the outside of the tank body; a separation cavity is formed between the dewatering coalescer and the left end of the tank body, and at least one oil removing coalescer is fixedly arranged in the separation cavity; a gap is formed between the top ends of the oil outlet collector and the dewatering coalescer and the inner wall of the tank body, an exhaust channel which can enable the separation cavity to be communicated with the liquid inlet cavity is formed, and an air outlet pipe is fixedly arranged on the tank body at the top end of the liquid inlet cavity; gaps are reserved between the bottom ends of the dewatering coalescer, the oil outlet collector and the oil removing coalescer and the inner wall of the tank body, and a liquid inlet sand removing channel penetrating through the bottom of the whole tank body is formed; at least two sand washing devices which can spray washing liquid and are parallel to the bottom of the tank body are fixedly arranged in the liquid inlet sand removing channel at intervals, each sand washing device is provided with a liquid inlet port, and the liquid inlet ports are positioned on the tank body and communicated with the outside of the tank body; a water outlet port is arranged on the tank body at the left end of the separation cavity above the left side of the liquid inlet desanding channel; a sand discharge pipe is fixedly arranged at the bottom of the tank body.
2. The high-temperature closed dehydration device according to claim 1 further comprising a heat energy centralized utilization unit, a glycol buffer tank, a glycol circulation pump; the cold source channel outlet of the first heat exchanger, the cold source channel outlet of the second heat exchanger, the cold source channel outlet of the third heat exchanger and the cold source channel outlet of the fourth heat exchanger are respectively communicated with the inlet of the heat energy centralized utilization unit through pipelines, the outlet of the heat energy centralized utilization unit is communicated with the inlet of the ethylene glycol buffer tank, the outlet of the ethylene glycol buffer tank is communicated with the inlet of the ethylene glycol circulating pump, the cold source channel inlet of the first heat exchanger, the cold source channel inlet of the second heat exchanger, the cold source channel inlet of the third heat exchanger and the cold source channel inlet of the fourth heat exchanger are respectively communicated with the outlet of the ethylene glycol circulating pump through pipelines.
3. A high-temperature closed dehydration device according to claim 1 or 2, characterized in that the dehydrator is a combined thermoelectric and chemical dehydration device or a high-temperature thermochemical dehydrator of super heavy oil or an electric dehydrator of super heavy oil high-temperature crude oil; or/and the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger all adopt ethylene glycol heat exchangers; or/and the high-temperature gas-carrying super-heavy oil slug flow trapping and processing integrated device is provided with a gas port capable of supplementing gas and relieving pressure.
4. A method for treating SAGD produced fluid by using the high-temperature closed dehydration device according to any one of claims 1 to 3, which is characterized by comprising the following steps: gas-liquid separation is carried out on the SAGD produced liquid with the temperature of 165-177 ℃ through a high-temperature steam-carrying super-thick oil slug flow trapping treatment integrated device to obtain degassed produced liquid and a gas phase containing steam and associated gas; the gas phase containing the steam and the associated gas is subjected to heat exchange and temperature reduction through a second heat exchanger; the method comprises the following steps that (1) after the degassed produced liquid is subjected to heat exchange and temperature reduction through a first heat exchanger, the temperature of the degassed produced liquid is kept in a supercooled state, the degassed produced liquid in the supercooled state enters an ultra-thick oil high-temperature high-efficiency elevation type pre-dehydration device for gel breaking treatment to obtain a water-containing oil phase and an oil-containing water phase, the water-containing oil phase enters a dehydrator for emulsion breaking and dehydration treatment to obtain purified oil and produced water, and the produced water and the oil-containing water phase enter a pressure oil remover for oil removal treatment to obtain oil; and the purified oil exchanges heat with the third heat exchanger for cooling, and the oil-removed produced water exchanges heat with the fourth heat exchanger for cooling.
5. The method of claim 4 where the temperature of the gas phase containing steam and associated gas is reduced from 165 ℃ to 177 ℃ to 85 ℃ to 90 ℃ after heat exchange in the second heat exchanger; or/and the temperature of the degassed produced fluid after heat exchange and temperature reduction by the first heat exchanger is kept in a state of supercooling from 20 ℃ to 22 ℃.
6. The method for treating SAGD produced fluid according to claim 4 or 5, wherein when the degassed produced fluid in the supercooled state enters the high-temperature high-efficiency elevation type pre-dehydration device for gel breaking treatment, gel breaker is added into the high-temperature high-efficiency elevation type pre-dehydration device for the super-thick oil, and the addition amount of the gel breaker is 80mg/L to 85 mg/L.
7. The method of treating a SAGD production fluid of claim 6, wherein the breaker is a polyether breaker.
8. The method for treating SAGD produced fluids of claim 4, 5 or 7, wherein the demulsifier is added to the dehydrator when the aqueous oil phase enters the dehydrator for demulsification and dehydration, and the dosage of the demulsifier is 100mg/L to 150 mg/L.
9. The method of claim 6 where the demulsifier is added to the dehydrator to add demulsifier to the aqueous oil phase when the oil phase enters the dehydrator for demulsification and dehydration, where the demulsifier is added at a rate of 100mg/L to 150 mg/L.
10. The method of treating SAGD production fluid of claim 8, wherein the demulsifier is a polyester demulsifier.
11. The method for treating SAGD produced fluid of claim 8, wherein the cold sources in the cold source channels of the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger are all ethylene glycol, the ethylene glycol after heat exchange and temperature rise enters the heat energy centralized utilization unit for heat energy recycling, and the ethylene glycol after heat energy recycling is reused as the cold source in the cold source channels of the first heat exchanger, the second heat exchanger, the third heat exchanger and the fourth heat exchanger for recycling.
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| CN105484716B (en) * | 2015-11-30 | 2018-01-02 | 中国石油天然气股份有限公司 | Oil field mining liquid heat-energy recovering apparatus and method |
| CN106014368B (en) * | 2016-06-27 | 2018-12-18 | 新疆石油工程设计有限公司 | Shallow super heavy oil SAGD high-temperature closed gathering and transporting device and its method |
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