WO2015081878A1 - Système de recyclage de la totalité de la boue à base d'huile à partir de déchets de forage sous forme de boue à base d'huile - Google Patents

Système de recyclage de la totalité de la boue à base d'huile à partir de déchets de forage sous forme de boue à base d'huile Download PDF

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Publication number
WO2015081878A1
WO2015081878A1 PCT/CN2014/093078 CN2014093078W WO2015081878A1 WO 2015081878 A1 WO2015081878 A1 WO 2015081878A1 CN 2014093078 W CN2014093078 W CN 2014093078W WO 2015081878 A1 WO2015081878 A1 WO 2015081878A1
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Prior art keywords
oil
mud
based mud
centrifugal
outlet
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PCT/CN2014/093078
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English (en)
Chinese (zh)
Inventor
王兵
黎跃东
任宏洋
张聪
邓存懿
Original Assignee
王兵
黎跃东
任宏洋
张聪
邓存懿
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Priority claimed from CN201320791340.1U external-priority patent/CN203741273U/zh
Priority claimed from CN201310645168.3A external-priority patent/CN103643910B/zh
Priority claimed from CN201320791189.1U external-priority patent/CN203669849U/zh
Application filed by 王兵, 黎跃东, 任宏洋, 张聪, 邓存懿 filed Critical 王兵
Publication of WO2015081878A1 publication Critical patent/WO2015081878A1/fr

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    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B21/00—Methods or apparatus for flushing boreholes, e.g. by use of exhaust air from motor
    • E21B21/06—Arrangements for treating drilling fluids outside the borehole
    • E21B21/063—Arrangements for treating drilling fluids outside the borehole by separating components
    • E21B21/065—Separating solids from drilling fluids

Definitions

  • the invention belongs to all oil-based mud wastes generated by oil-based mud drilling operations in shale gas, tight gas, tight oil and conventional oil and gas field exploration and development process, including oil-based cuttings and vibrating screen leakage generated during oil-based mud drilling. Slurry, cementing back-mixing slurry, plugging and returning waste slurry, completion tank clearing mud, sewage containing oil-based mud, glove-wood cobblestone contaminated with oil-based mud, etc., all oil-based waste, harmless treatment
  • the invention relates to the field of oil-based mud resource recycling and recycling, in particular to a treatment and recovery system for synchronously recovering oil-based mud in oil-based mud drilling waste.
  • the base oils of commonly used drilling oil-based muds include diesel-based, white oil-based and synthetic base oil bases.
  • Oil-based mud is based on diesel oil, white oil, bio-oil, synthetic oil, etc., and various oilfield chemicals are added. It is a commonly used oil-based mud type in the world. Oil-based mud drilling wastes are generated during oil-based mud drilling, mainly including oil-based cuttings, vibrating screen leakage, cementing back-mixing, plugging and returning waste slurry, completion of clearing tank sediment, and oil-based mud. Sewage, debris contaminated by oil-based mud, etc.
  • the single well production volume is about 250-600m3, and the oil-based mud volume is about 18-25%.
  • the oil-based mud drilling waste contains huge economic value and should be oil-based mud recovery.
  • Waste oil-based drilling mud rock The liquid phase in the scrap mainly includes base oil base and mud additive; the solid phase mainly includes: such as barite powder, broken rock cuttings, and the solid phase particle size distribution is wide, ranging from the particle size distribution to the order of centimeters to centimeters.
  • Mud tank bottom mud is mainly a part of oil-based mud remaining in the mud tank.
  • the liquid phase mainly includes base oil base and mud additive.
  • the solid phase mainly includes: such as barite powder and ultrafine cuttings, alumina powder.
  • the particle size of the solid phase is small, generally 10 um.
  • This kind of oil-based mud waste is a complex multi-phase system containing mineral oil, phenolic compounds, etc.
  • the main pollutants come from the base oil of oil-based mud and the main and auxiliary emulsion additive base.
  • the commonly used oil base includes diesel oil. Base, white oil base and synthetic base oil base.
  • waste oil-based mud and oil-based mud drill cuttings are subject to post-treatment.
  • waste oil-based mud and oil-based drill cuttings have been incinerated, cracked, and biodegraded.
  • the incineration method has large capital investment, high operating cost, and the exhaust gas generated during the incineration process is likely to cause a second environmental pollution;
  • the landfill method has less investment, but it does not really eliminate diesel-like pollutants in oil-containing cuttings.
  • the object of the present invention is to provide a low-cost, non-secondary pollution and recoverable expensive oil-based mud resource, and simple operation to recover all oil base from oil-based mud drilling waste.
  • the mud system realizes the maximum recovery of oil-based mud resources; the oil-based mud drilling waste includes diesel-based, white oil-based and synthetic-based waste oil-based drilling mud, mud tank bottom mud, cementing slurry, and plugging High-oil drilling wastes such as waste slurry and oil-containing cuttings.
  • the oil-based mud drilling and oil-based system of the present invention recovers an oil-based mud and oil-based system, including an oil-based mud centrifugal separation subsystem and a deep desorption and recovery oil-based mud subsystem at a normal temperature.
  • An oil-based mud and oil-based system is recovered in the oil-based mud drilling waste of the present invention, the oil-based mud centrifugal separation subsystem comprising a centrifugal filtration process, a homogenization process and a centrifugal sedimentation process; the homogenization process is to centrifugally settle
  • the oil-based mud produced in the process is partially returned to the buffer tank and mixed with the coarse separation mud produced during the centrifugal filtration process. After homogenization, it is centrifuged and separated into centrifugal sedimentation process, wherein the reflux ratio is 1:1-2.5: 1.
  • the homogenization process is to set a mud solid content detecting instrument and a mud viscosity detecting instrument in the buffer tank, and mix and homogenize the coarse separation mud obtained by centrifugal filtration and the subsequent centrifugal sedimentation separation to homogenize the mixture to make the mixture density, viscosity,
  • the solid content and other properties are stable and reach the requirements of the centrifugal sedimentation equipment at the back end, and then pumped into the centrifugal sedimentation equipment.
  • the homogenization process in the buffer tank is carried out by returning the qualified mud produced by centrifugal sedimentation to the coarse separation mud produced by centrifugal filtration, and the reflux ratio is 1:1-2.5:1.
  • An oil-based mud system is recovered from the oil-based mud drilling waste of the present invention, which also includes a feed filtration process prior to the centrifugal filtration process.
  • a feed filtration process prior to the centrifugal filtration process.
  • the feed section has a feed screen which has a pore size of 4-6 cm to prevent foreign matter from entering the centrifugal filtration equipment, causing clogging and pre-separation of materials.
  • the oil-based mud drilling waste of the present invention recovers the oil-based mud and oil-based system
  • the centrifugal filtering device included in the centrifugal filtration process has a rotation speed of 600-2400r/min, and the rotation speed thereof is preferably 600-900r/min;
  • the centrifugal filter device has a filter pore size of 0.2-5 mm, wherein preferably the filter mesh has a pore diameter of 0.8-4 mm; and the material retention time in the centrifugal filtration is 5-30 s.
  • a tapered cross section is adopted, and the taper angle is 30-60 degrees.
  • the tapered cross-section mesh hole can prevent the solid phase from blocking the mesh and improve the centrifugal filtration efficiency.
  • the residence time of the material in the centrifugal filtration is 5-30 s, and the residence time of the centrifugal filtration material can further be 6-25 s.
  • the mud drilling abandonment ratio is large, the viscosity is large, the particle size distribution is wide, and the particle size is high.
  • the centrifugal force at the rotation speed is large, which is conducive to the filtration of the liquid.
  • the coarse separation mud obtained by the centrifugal filtration has a high solid content, a large sand content, a large viscosity, a solid content of about 60-65%, a solid phase maximum particle diameter of about 5.5 mm, and a median diameter of about 0.05-0.1mm, demulsification voltage ES is 420-500mV, mud viscosity is >500s, and the results of six-speed (3, 6, 100, 200, 300, 600r/min) are: (18-25)/(26- 50) / (180-240) / (> 300) / (> 300) /> (300), can not reach the oil-based mud reuse performance indicators, need to be transported into the buffer tank, mixed, homogenized and further processed.
  • An oil-based mud and oil-based system is recovered from the oil-based mud drilling waste of the present invention, wherein the centrifugal speed of the centrifugal sedimentation device during the centrifugal sedimentation process is 600-3000 r/min, preferably 900-2400 r/min;
  • the differential speed of the pusher spiral is ⁇ 600r/min, and the differential speed is preferably ⁇ 300r/min.
  • the centrifugal solidification system has a feed solid content of 30%-50% and a feed slurry viscosity of ⁇ 400s.
  • the solid phase particles having a higher density than the liquid phase rapidly settle to the inner wall of the drum under the strong centrifugal force of the drum, and are deposited by the auger.
  • the solid phase of the inner wall of the drum is pushed to the compression section of the small end of the drum, and is further squeezed, deliquored, and discharged through the slag outlet in the process, and the separated qualified slurry flows out from the overflow end of the drum.
  • the qualified mud enters the buffer tank and is mixed with the coarse mud slurry filtered by the centrifugal filter.
  • the treated mixed mud then enters the centrifugal sedimentation equipment for sedimentation.
  • a part of the qualified mud flows back into the buffer tank, and part of the slurry is recovered. Recycling using standard mud.
  • Qualified mud is the standard that has not yet been recycled, but it is in line with the mud that is returned to the buffer tank.
  • the mud recovery rate can reach more than 60%, and the solid content of the oil base produced by the two-stage centrifugal separation is 10-20%, and the maximum solid phase particle diameter is about 50-80 um.
  • the particle size is about 10-30um
  • the demulsification voltage ES is 700-2000mV
  • the mud viscosity is 100-150s
  • the six-speed (3, 6, 100, 200, 300, 600r/min) results are: (6-10) /(12-40)/(50-80)/(90-120)/(130-180)/(240-400)
  • the recovered oil base can be recovered and reused in drilling engineering.
  • the content of pollutants in the solid phase separated is greatly reduced, and the petroleum content is ⁇ 10%, which has significant economic benefits. Suitable for treating used oil-based mud or oil-containing cuttings.
  • the invention aims at the characteristics that the solid particle size difference in the waste oil-based mud is large and the solid phase density difference is large, and the centrifugal filtration and the centrifugal sedimentation process are coupled, and the 0.25-2 cm solid phase particles in the mud are removed by centrifugal filtration.
  • Centrifugal sedimentation removes 0.1-1.5mm solid phase particles in the mud, and through the control of process parameters, ensures that the performance of the recovered oil-based mud meets the requirements of drilling engineering reuse, which can effectively separate and recover a large amount of oil-based mud, and has strong
  • the anti-wear and clogging ability, and the system operation stability and reliability are better.
  • the high mud recovery rate reduces pollutant emissions and achieves the unification of economic and environmental benefits.
  • An oil-based mud and oil-based system for recovering oil-based mud drilling waste of the present invention the agent is deeply desorbed at room temperature, and the oil-based mud subsystem includes a deep desorption process at a normal temperature, a distillation condensation process, and a distillation process during the condensation process. The medicament is then returned to the process of recycling during the deep desorption process at room temperature.
  • An oil-based mud and oil-based system is recovered from the oil-based mud drilling waste of the present invention.
  • the deep desorption step of the agent at room temperature is to put the agent into the reactor from the top of the reagent reactor, and the ratio of the agent to the solid phase is 0.7.
  • the ratio of /1-1/1 is added, the top of the reagent reactor is placed in the reactor, and the deep desorption time is 10-40 min; the oil-containing agent is discharged from the liquid outlet on the reactor, enters the buffer tank, and the fine powder after sedimentation
  • the drain outlet at the bottom of the buffer tank is discharged; the liquid outlet on the reactor is located 0.2-0.5 m from the bottom.
  • the oil-based mud drilling oil and the oil-based system are recovered from the oil-based mud drilling waste of the present invention, and the deep desorption step of the chemical agent at the normal temperature further includes a combined backflushing process of the medicament and the nitrogen, and the part of the recovered medicament is pumped from the backflushing pipeline by the pump.
  • the pump At the bottom of the reactor, stir the fine powder deposited on the tapered surface of the bottom of the reactor to form a flowable suspension with the agent, the recoil strength is 8-10L/m 2 .s, and the rinsing time is 5-8 minutes. Then pump it out of the liquid outlet and circulate continuously.
  • the oil-based mud drilling oil and the oil-based system are recovered in the oil-based mud drilling waste of the present invention, and the deep desorption step of the chemical agent at the normal temperature further comprises driving nitrogen gas with a certain pressure of 1.5-2.5 MPa into the reactor through the tee in the liquid outlet.
  • the bottom tapered surface cleans the powder that blocks the liquid outlet.
  • the oil-based mud drilling oil and the oil-based system are recovered in the oil-based mud drilling waste of the present invention, wherein the steam is heated by steam at a temperature of 110-125 ° C, the steam pressure is 1-4 kg, and the steam is heated by a heat exchanger.
  • the drug mixture is brought to 70-80 ° C; in the condensation step, the condensation temperature is 40-45 ° C, and the recovery of the drug after condensation is >90%.
  • the condensing unit comprises a two-stage condensation process
  • the first-stage condensation process may be a circulating water cooling device, an air cooling device or an evaporating condenser, a condensation temperature of 20-40 degrees Celsius, and a recovery rate of the agent after condensing >94%, level 2
  • the condensation process is an air chilling device with a condensing temperature of 5-8 degrees Celsius. After condensing, the recovery rate of the agent is >98%, and the condensed recovered agent can be recycled to the reactor again through the pump.
  • the solid phase separated from the desorption reactor is sent to a solid phase de-container, heated by steam, steam temperature 110-125 ° C, steam pressure 1-4 kg, controlled gas phase temperature 90 ° C, solid
  • the phase residence time is 30-50 min.
  • the chemical vapor generated by the solid phase deaeration enters the condensing device, and condenses and recovers the chemical vapor generated during the drying process.
  • the solid phase desorption reactor is connected to the condensing device, and the introduced nitrogen gas enters the condensing device to condense and recover the blown off chemical vapor, thereby recovering a small amount of vaporized chemical during the reaction.
  • An oil-based mud and oil-based system for recovering oil-based mud drilling waste of the present invention comprising a vibrating screen connected to the feed port, the side of the vibrating screen being provided with a connection to the closed scraper conveyor a conical hopper No. 1 having a No. 2 conical hopper connected to the centrifugal filter below the vibrating screen; the mud outlet of the centrifugal filter is connected to a homogenizing buffer tank, and the output port of the homogenizing buffer tank is connected To the centrifugal sedimentation device No. 1, the mud outlet of the No. 1 centrifugal sedimentation device is connected to the homogenization tank, and the solid phase outlet of the No. 1 centrifugal sedimentation device is connected to the No.
  • the mixed liquid outlet of the reactor is connected to a centrifugal sedimentation device No. 2; the solid phase outlet of the centrifugal filter is connected to a closed scraper conveyor, and the closed scraper conveyor is connected to a deep desorption reactor No. 1;
  • the solid phase outlet of the No. 1 deep desorption reactor is connected to a closed conveyor, the liquid phase outlet of the No. 1 deep desorption reactor is connected to the No. 2 centrifugal sedimentation device, and the solid phase outlet connection of the No. 2 centrifugal sedimentation device To the closed conveyor,
  • the closed conveyor is connected to a dry desolvation machine; the liquid phase outlet of the No. 2 centrifugal sedimentation device is connected to the No.
  • the liquid outlet of the No. 1 evaporator is connected to the No. 2 evaporator, the 2
  • the oil-based mud outlet of the evaporator is connected to the oil-based mud tank; wherein the steam inlets of the No. 1 evaporator, the No. 2 evaporator, and the dry desolventizer are respectively connected to the steam boiler.
  • the evaporation process is heated by steam, with a steam temperature of 110-125 ° C and a steam pressure of 1-4 kg.
  • the first-stage evaporator is a unipolar continuous flow evaporator, heating the oil-containing agent mixture to 50-90 ° C, evaporating to make the content of the agent in the mixture ⁇ 40%, and the medicament vapor enters the condensing device.
  • the mixture is pumped into the stage 2 evaporator.
  • the 2-stage evaporator is for heating the oil-containing agent mixture to 70-90 ° C, evaporating to make the agent content of the mixture liquid ⁇ 1%, the medicament vapor enters the condensing device, and the remaining liquid phase in the reactor is tested and passed as a qualified oil.
  • the base mud is pumped into the oil-based mud storage tank.
  • the oil-based mud and oil-based system of the oil-based mud drilling waste of the present invention the steam outlet of the No. 1 evaporator, the No. 2 evaporator and the dry desolvation machine, and the solvent vapor of the No. 1 deep desorption reactor
  • the outlets are respectively connected to a condenser, the solvent fluid outlet of which is connected to a solvent storage tank, the outlet of which is connected to the solvent inlet of the No. 1 deep desorption reactor and the No. 2 deep desorption reactor,
  • the circulating cooling water inlet of the condenser is connected to a condenser refrigerator, which is connected to a cooling water buffer tank whose circulating cooling water outlet is connected to a cooling water buffer tank.
  • an oil-based mud and an oil-based system are recovered, and a slurry outlet of the centrifugal sedimentation device No. 1 is connected to a homogenization tank and a mud tank, and a discharge port of the dry de-dissolving machine is connected to Conveyor.
  • An oil-based mud and oil-based system is recovered in the oil-based mud drilling waste of the present invention, wherein the No. 1 evaporator is provided with a stirring paddle, the agitating paddle is connected to an output shaft of the motor, and the motor is disposed on the evaporator
  • the top of the evaporator is provided with a manhole and a solvent vapor outlet connected to the condenser, and an annular heating steam heating tube is arranged in the evaporator No. 1, and the steam heating pipe is connected with steam condensation a liquid outlet connected to the steam inlet of the steam boiler, the steam inlet connected to the middle side wall, the vapor condensate outlet being disposed at a lower side wall of the No. 1 evaporator, and a drain at the bottom of the No. 1 evaporator hole.
  • An oil-based mud and oil-based system is recovered from the oil-based mud drilling waste of the present invention, wherein the drying and desolventizing machine is provided with a steam heating plate for drying, and a steam is provided on the side wall of the drying and desolventizing machine.
  • a condensate outlet and a steam inlet connected to the steam boiler, wherein the steam heating plate is respectively connected to the steam inlet and the steam condensate outlet, and a feed port and a steam outlet are arranged at the top of the desolventizer, and the drying is off
  • the bottom of the melting machine is the discharge port, and a discharge motor is arranged at the discharge port.
  • An oil-based mud and oil-based system is recovered from the oil-based mud drilling waste of the present invention, and the inner top of the No. 1 deep desorption reactor is provided with a solvent spray device connected to a solvent storage tank, the solvent spray A filter screen is arranged under the device, the filter screen is provided with a scraper plate, the edge of the filter screen is aligned with the inlet of the screw conveyor, and the solid discharge port of the screw conveyor is set at No. 1 Outside the deep desorption reactor, the top of the No. 1 deep desorption reactor is provided with a solid feed port and a solvent vapor outlet connected to the condenser.
  • An oil-based mud and oil-based system is recovered in the oil-based mud drilling waste of the present invention, wherein the No. 2 deep desorption reactor is provided with a stirring paddle, and the stirring paddle is connected to an output shaft of the stirring motor, the stirring The motor is disposed at the top of the No. 2 deep desorption reactor, and a solid phase material inlet, an observation hole, and a solvent vapor outlet connected to the condenser are disposed at the top of the No. 2 deep desorption reactor, at the depth of No. 2 A manhole is provided on the side wall of the desorption reactor, and the bottom of the No. 2 deep desorption reactor is provided with a drain hole and a liquid outlet connected to the No. 2 centrifugal sedimentation device.
  • the medicament recovered in the distillation condensation process is returned to the process of recycling in the deep desorption process at normal temperature, and the solid phase separated from the desorption reactor is sent to the solid phase decontamination vessel, and heated by steam, the steam temperature is 110-125 ° C. , steam pressure 1-4 kg, control gas temperature Degree 90 ° C, solid phase residence time 30-50min.
  • the chemical vapor generated by the solid phase deaeration enters the condensing device, and condenses and recovers the chemical vapor generated during the drying process.
  • the solid phase desorption reactor is connected to the condensing device, and the introduced nitrogen gas enters the condensing device to condense and recover the blown off chemical vapor, thereby recovering a small amount of vaporized chemical during the reaction.
  • the oil-based mud obtained after evaporation of the separation agent has a solid content of ⁇ 10%, a ratio of oil to water of 9:1, a maximum solid phase particle diameter of about 50-80 um, a median diameter of about 10-30 um, and a liquid viscosity of ⁇ 60 s. Can be reused as an oil-based mud to the drilling site.
  • the system for recovering all oil-based mud from oil-based mud drilling waste wherein the reaction process can synchronously recover oil-based mud from oil-based mud drilling waste, thereby maximizing the resource recovery of expensive oil-based mud
  • the oil-based mud recovery rate is >99.7%, which creates greater economic value.
  • it realizes the harmless standard treatment of oil-containing wastes.
  • the oil content in the solid phase is ⁇ 0.3%, and the reaction reagent used can be recycled and reused.
  • the dosage of the medicament is low, and the treatment process is carried out under normal temperature and normal pressure.
  • the treatment time is short, there is no second pollution, equipment investment and operation cost are low, and significant environmental, social and economic benefits are obtained.
  • FIG. 1 is a process flow diagram of the present invention
  • Figure 1 is a schematic view of a recycling apparatus of the present invention
  • Figure 3 is a schematic view showing the structure of the evaporator No. 1 in the present invention.
  • Figure 4 is a schematic view showing the structure of the drying and desolventizing machine of the present invention.
  • Figure 5 is a schematic view showing the structure of a deep desorption reactor No. 1 in the present invention.
  • Fig. 6 is a schematic view showing the structure of a deep desorption reactor No. 2 in the present invention.
  • the system for recovering all the oil-based mud from the oil-based mud drilling waste of the present invention wherein the recovery equipment is as shown in FIG. 2, wherein the vibrating screen 1 is connected to the feed port, and the foreign matter such as the stone in the upper part of the vibrating screen 1 passes through the No. 1
  • the conical hopper 2 is connected to the closed squeegee conveyor 3, and the lower mud of the vibrating screen 1 is connected to the centrifugal filter 5 through the No. 2 conical hopper 4, and the solid phase outlet of the centrifugal filter 5 is connected to the sealing squeegee conveyor 3, and is sealed.
  • the outlet of the scraper conveyor 3 is connected to the desorber No.
  • the liquid phase of the centrifugal filter 5 is pumped by the mud pump 6 into the homogenization buffer tank 7, and the liquid phase outlet of the homogenization buffer tank 7 is passed through the mud pump 8 and No. 1
  • the decanter centrifuge 9 is connected.
  • the liquid phase outlet of the No. 1 decanter centrifuge 9 is connected to the mud pump 10, and the lines of the mud pump 10 are connected to the homogeneous buffer tank 7 and the mud tank 11, respectively; the solid phase outlet is connected to the reaction tank 12.
  • the mixed liquid outlet of the reaction tank 12 is connected to the mud pump 13 and connected to the No. 2 horizontal screw centrifuge 14 through a pipeline.
  • the liquid phase outlet of the No. 2 horizontal screw centrifuge 14 is connected to the mud pump 16 and connected to the No.
  • the evaporator 17 is connected to the pump 18 and is connected to the evaporation tank No. 19.
  • the evaporation tank 19 is connected to the pump 20 and is connected to the oil-based mud tank 21.
  • the solid phase outlet of the No. 1 desorber 10 The solid phase outlet of the No. 2 decanter centrifuge 14 is connected to the closed conveyor 15 and is connected to the dry desolventizer 22. After the drying and desolventizing machine 22 is dried, the solid phase outlet is connected to the conveyor 23, and the dried solid phase is conveyed to the stack.
  • the solvent tank 24 is connected to the solvent pump 25, and is redistributed to the reaction tank 12 and the desorber No. 1.
  • the gas lines are all connected to a condenser 26 which is connected to the solvent tank 24 after condensation.
  • the condenser 26 is connected to a refrigerator 27 which is connected to the cooling water tank 29 via a pump 28.
  • the boiler is connected to the desolvation unit 22 via a steam line.
  • a motor 38 is disposed above the evaporator 17 of the first stage, and is mounted on the motor support for driving the stirring paddle, and the 34 is rotated.
  • the solvent vapor outlet 31 and the inspection hole 38 are disposed above the evaporator No. 1 and the evaporator No. 1 is provided. 17
  • the central facility steam inlet 32 and the observation hole 37 are provided with a steam heating pipe 33 in the evaporator No. 1, and a drain hole 35 and a steam condensate outlet 36 are provided at the bottom of the No. 1 evaporator 17.
  • the structure of the evaporator No. 2 is the same as that of the evaporator No. 1.
  • the upper portion of the drying and desolventizing machine 22 is provided with a feed port 39, a steam heating plate 43 is disposed inside, a steam inlet 40 and a steam condensate outlet 42 are disposed at the middle, and a motor 41 is disposed below.
  • the No. 1 desorber 10 is provided with a solid feed hole 51 and a solvent vapor outlet 50.
  • the upper part of the desorber is provided with a solvent spraying device 49, and a filter screen 44 is disposed on the upper part of the desorber, and the scraping plate 48 is provided.
  • the solids are pushed forward on the screen until the large particulate solids fall into the auger 45, and the desorbed large particulate material is conveyed by the auger to the solids discharge port 47.
  • the small particles and solvent pass through the filter screen 44 to the bottom of the desorber, and a liquid outlet 46 is provided at the bottom of the desorber.
  • a motor 52 is disposed above the No. 2 desorber 12, and is mounted on the motor support for driving the stirring paddle 59 to rotate.
  • the No. 2 desorber 12 is provided with a solid phase material inlet 52, a solvent vapor outlet 57 and an observation.
  • the hole 58, the manhole 54, and the liquid hole 56 and the drain hole 55 are provided at the bottom.
  • the system for recovering all the oil-based mud from the oil-based mud drilling waste is operated in the following manner: the feeding port is connected with the vibrating screen 1, and the foreign matter such as stones in the upper part of the vibrating screen passes through the No. 1 cone hopper 2
  • the sealing blade conveyor 3 enters the desorber 10 through the sealing blade conveyor 3 to perform a desorption section; the lower mud of the vibrating screen enters the centrifugal filter 5 through the No. 2 conical hopper 4 for centrifugal filtration.
  • the solid phase produced by the centrifugal filtration is sent to the desorber 10 through the sealing blade conveyor 3 to perform the desorption section; the coarse separation slurry produced by the centrifugal filter 5 is pumped by the mud pump 6 into the homogenizing buffer tank 7.
  • the homogenization buffer tank 7 functions as a buffer and homogenizes, and the coarse separation mud produced by the centrifugal filter 5 is mixed with the qualified mud produced at the back end to be homogenized, and the feed into the No. 1 decanter centrifuge 9 is obtained.
  • the mud pump 8 is pumped into the No. 1 decanter centrifuge 9 for centrifugal sedimentation separation.
  • the slurry separated by the No. 1 decanter centrifuge 9 reaches the reuse standard, it enters the mud storage tank 11 through the mud pump 10, partially returns to the homogenization tank 7; the separated solid phase enters the No. 2 desorber 12.
  • the solvent is pumped into the applicator 12, and is thoroughly mixed and reacted with the separated solid phase, and the mixed liquid is pumped through the mud pump 13 into the No. 2 decanter centrifuge 14.
  • the solvent and the solid phase material generated by the vibrating screen 1 and the centrifugal filter 5 are mixed.
  • the liquid phase containing the small particles enters the No. 2 decanter centrifuge 14, and the large particle solid is solid.
  • the phase enters the dry desolventizer 22.
  • the oil-containing solvent separated by the No. 2 decanter centrifuge 14 is pumped into the No. 1 evaporator for preliminary concentration, and then pumped into the No.
  • the system for recovering all oil-based mud from the oil-based mud drilling waste wherein the vibrating screen is used for removing large-sized foreign matter in the waste, preventing and blocking the pipeline and the subsequent equipment, and the mesh aperture is 2-3 cm.
  • the vibration frequency is 180-200r/min, and the vibrating screen is installed at a tilt of 40-50 degrees.
  • the horizontal centrifugal filter has a centrifugal speed of 600-750 r/min in centrifugal filtration and a filter mesh diameter of 1.5-2.0 mm.
  • the liquid phase after the centrifugal filtration is a crude separation slurry
  • the solid content of the crude separation mud is 50-80%
  • the median diameter of the solid particles is 0.2-0.5 mm
  • the viscosity is >750 s
  • the solid phase after the centrifugal filtration is a large particle.
  • the homogenization buffer tank is equipped with a stirrer, the stirrer speed is 30-50r/min, and the homogenization buffer tank
  • the mud solid content detecting device and the mud viscosity detecting device are set, and the coarse separated mud and the back-end separated separated qualified mud are mixed and homogenized, and the homogenized mud solid particles are contained in the range of 30%-50%, the feed mud viscosity ⁇ 400s, the median diameter of the solid particles is 0.1-0.2 mm, and the homogenized crude separated oil-based mud is pumped into the centrifugal sedimentation device by a mud pump.
  • the centrifugal sedimentation device adopts a horizontal screw centrifuge, the rotating speed of the horizontal rotating centrifuge is 2000-3500r/min, and the differential speed of the rotating drum and the pushing material is ⁇ 300r/min. After the pretreatment treatment and recovery process, the mud recovery rate can reach 60-70%. After two-stage centrifugal separation, the solid content of the oil base is 10-20%, and the maximum solid phase particle size is about 50-80um. The particle size is about 10-30um, the demulsification voltage ES is 700-2000mV, the mud viscosity is 100-150s, and the recovered oil base can be recovered and reused in drilling engineering. The small particles separated by the centrifugal sedimentation have an oil content of 8-10%, enter the rear end No.
  • the oil-based recovered low oil-containing solid phase desorption-evaporation apparatus includes: a solvent storage tank, a pusher, a desorber, a dryer, an evaporator, a condenser, and the like.
  • the low oil-containing solid phase is subjected to material transportation, solvent desorption, solid-liquid separation and solid drying steps to realize the analysis of the solid phase surface oil-based mud;
  • the resulting oil-containing solvent mixture is subjected to evaporation-condensation to recover the solvent, and the recovered solvent is recycled to realize the recovery of the oil-based mud in the low oil-containing solid phase.
  • the centrifugally filtered large particle cuttings enter the No. 1 desorber through a closed auger, and the solvent and the cuttings particles are added according to a volume ratio of 1:1 to 1:1.5, and the desorption time is 10-15 min.
  • the sieve plate is arranged in the No. 1 desorber, the sieve plate has a hole diameter of 0.8-1 mm, and the large particle solid phase is transported to the dryer through the screw conveyor, and the separated solvent and the oil-based mud mixture are transported to the No. 1 evaporation through the solvent pump. Device. After the centrifugal filtration, the small particle solid phase enters the No. 2 desorber through the hopper, the solvent and the small particle solid phase volume ratio are 1:2-1:3, and the solid residence time in the No. 2 desorber is 20 -30min.
  • the 2 desorption tank is equipped with a stirrer, the stirrer rotates at a speed of 50-60 r/min, and the mixed liquid is pumped into the decanter centrifuge through a mud pump.
  • the solid phase is transported to the dryer, and the separated solvent and oil-based mud mixture is delivered to the No. 1 evaporator through the solvent pump.
  • the No. 1 evaporator is heated by steam, the steam temperature is 110-125 degrees Celsius, the steam pressure is 1-4 kilograms, the steam is heated by the heat exchanger to heat the oil-containing solvent mixture to 40-50 degrees Celsius, and the preheated mixture is pumped into the No.
  • the evaporator, solvent vapor enters the condensing system through the line.
  • the No. 2 evaporator is heated by steam, the steam temperature is 110-125 degrees Celsius, the steam pressure is 2-3 kilograms, the steam is heated by the heat exchanger to heat the oil-containing solvent mixture to 70-80 degrees Celsius, and the solvent vapor enters the condensation system through the pipeline to complete the evaporation.
  • the oil-based mud of the process is pumped through the pipeline into an oil-based mud storage tank.
  • the dry desolventizer is heated by steam, the steam temperature is 110-125 degrees Celsius, the steam pressure is 1-1.5 kilograms, the solid is heated to 70-80 degrees Celsius, and the solvent vapor enters the condensation system through the pipeline.
  • the condenser is cooled by circulating water, the condensation temperature is 18-20 degrees Celsius, and the solvent recovered by condensation is flowed through the pipeline to the solvent storage tank.
  • the solvent storage tank is provided with a solvent pump, and the solvent recovered by the condensation is pumped into the front end No. 1 desorber and the No. 2 desorber to realize the recycling of the solvent.
  • the mud oil and oil-based recovery equipment of the waste oil-based mud of the invention can realize the harmless treatment of oil-based mud or drill cuttings, and can recover most of the oil-based mud in the oil-based mud or drill cuttings to realize resources. Recycling and harmless treatment of waste; through the system, oil-based mud recovery and oil-based mud recovery can be realized, resource recovery rate is >90%; oil content of solid waste treated by the invention is ⁇ 1%; production The solvent is recycled during the process without secondary pollution.
  • the process steps in the present invention include: the process recovery process includes centrifugation, deep desorption of the agent at room temperature, and condensation condensation, and a process for recycling the drug.
  • the operation mode is that the feed port is connected with the vibrating screen, and the foreign matter such as stones on the upper part of the vibrating screen enters the reactor through the conveyor, and is sent to the dryer after the deep desorption section of the agent at normal temperature; the liquid slurry in the lower part of the vibrating screen enters the centrifugal filter Centrifugal filtration was carried out.
  • the solid phase produced by centrifugal filtration is transported to the reactor through the conveyor, and is discharged to the dryer after the deep desorption section of the medicament at normal temperature; the coarse separation mud produced by the centrifugal filter can be pumped into the homogenization buffer tank.
  • the homogenized buffer tank plays the role of buffering and homogenizing.
  • the coarse separation mud produced by the centrifugal filter is mixed with the qualified mud produced at the back end, and homogenized.
  • the pump After reaching the feeding standard of the horizontal screw centrifuge, the pump is placed in the bed.
  • the snail centrifuge is centrifuged and separated, and the solid phase separated by the horizontal centrifuge is transported to the reactor through the conveyor.
  • the separated liquid phase is a qualified slurry, partially enters the mud storage tank, and partially returns to the homogenization tank.
  • the solid phase separated by the vibrating screen, centrifugal filter and centrifugal sedimentation equipment enters the reactor, and the agent is fully mixed with the low oily solid in the reactor, and the solid-liquid separation is carried out through the internal sieve of the reactor, and the large particle solid phase enters.
  • the drying and desolventizing machine, the liquid phase containing small particles enters the decanter centrifuge, and the solid liquid is carried out by the decanter centrifuge, and the separated solid small particles enter the dryer to be dried, and the separated liquid phase oil-containing medicament enters the No. 1 evaporator for preliminary concentration. Then, enter the No.
  • the solids conveying device can be a screw conveyor, a chain conveyor or a closed conveyor belt.
  • the solid-liquid separation device may be a closed centrifugal settler or a closed filter press.
  • This embodiment is located in an oil-based mud drilling project in an oilfield in Xinjiang.
  • diesel-based drilling mud is used in the treatment project of waste oil-based mud and oil-containing cuttings.
  • the drilling formation is sandstone.
  • the particle size of the cuttings is small, and the mechanical strength of the particles is relatively high. Low, easy to break during the centrifugation process.
  • the process includes centrifugation, reagent reaction, and distillation condensation.
  • the design verification process scale was 0.8m 3 /h, and the treatment capacity, treatment effect and process stability of the process were investigated.
  • the raw material is first pre-separated through a feed screen.
  • the mesh size is 6 cm.
  • the maximum solid particle size is 5.6 cm
  • the median diameter is about 1.0 mm
  • the solid phase liquid content is about 16. %.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • Centrifugal filtration is carried out by centrifugal filtration using a variable frequency centrifugal filter.
  • the separation of large particle cuttings and oil-based mud is achieved mainly by centrifugal force and interception through the screen.
  • the filter screens with 0.5mm, 0.8mm, 1.5mm, 2.0mm and 4.0mm apertures are integrated for centrifugal filtration.
  • the centrifugal speed is 800r/min.
  • the effect of centrifugal filtration with different apertures is shown in the table.
  • the filter aperture is 2mm.
  • the key process index the treatment volume reaches 0.92m 3 /h, the liquid phase recovery rate reaches the maximum value of 25%, and the separation solid phase oil content rate reaches 6%.
  • the 2 mm pore size filter screen has a higher filtration efficiency as shown in Table 1.
  • the general centrifugal filtration process mainly utilizes a small filtration gap and forms a thick filter cake layer, and utilizes the interception of the filter cake layer to achieve solid-liquid separation.
  • the waste drilling and completion fluid ratio is large and the viscosity is large.
  • the general centrifugal filtration process has great limitations.
  • the liquid phase has a large centrifugal force in the drum, which is favorable for solid-liquid separation.
  • the output spiral speed is faster, the residence time of the material in the drum is shorter, and the separation efficiency is poor.
  • the too fast rotation speed causes the filter cake layer to form relatively dry and is relatively hard, resulting in poor separation efficiency at a later stage, and the filter cake layer formed at a lower rotation speed is looser, which is favorable for liquid phase separation.
  • the higher rotational speed of the centrifugal force is larger, which is conducive to the filtration of the liquid, but the excessively high rotational speed is easy to grind the material, the ground material is further mixed with the mud cake, the effect of effectively separating the solid particles is poor; and the higher rotation speed leads to the spiral
  • the discharge rate is increased, the residence time of the material in the drum is short, and the separation efficiency is poor.
  • the too fast rotation speed causes the filter cake layer to form relatively dry and relatively hard, resulting in poor separation efficiency at a later stage, so the filter cake layer formed at a lower rotation speed is looser, which is favorable for the separation of the liquid phase.
  • the key parameters of the process are 0.92m 3 /h, the liquid recovery is 28%, and the solid phase is 6%.
  • the separated solid phase particles are larger, which is beneficial to the subsequent reaction section, the system runs smoothly, and a good balance is obtained between the two key parameters of the treatment volume and the quality of the coarse separation mud.
  • Other parameters of the process operation include the solid separation of the crude separation slurry obtained by centrifugal filtration of about 47%, the maximum particle size in the solid phase of about 4.5 cm, the median diameter of about 0.08 mm, and the demulsification voltage ES of 415 mV. 500s,
  • the homogenized slurry in the buffer tank is pumped into the centrifugal settling device through the mud pump.
  • the solid-liquid separation effect of centrifugal sedimentation under different drum rotation conditions was tested, as shown in Table 3 above.
  • the low oil-containing solid phase is subjected to a desorption process at a normal temperature and deep desorption process to achieve the removal of oil in the solid phase.
  • the desorbent agent is added to the desorption unit at a ratio of 0.7:1 by mass ratio.
  • the clear liquid is pumped into the chemical circulation subsystem, and the solid content in the liquid phase is ⁇ 15%, and the separated solid enters the solid phase desolvent reactor.
  • the large-particle solid is transported to the solid desolventizer; the solid content in the separated liquid phase is ⁇ 15%, which is a drug-oil-based mixture, and enters the solvent. Loop subsystem.
  • the evaporation device includes a 1-stage evaporator and a 2-stage evaporator.
  • the evaporation process is heated by steam, with a steam temperature of 110-125 degrees Celsius and a steam pressure of 0.7-0.8 kilograms.
  • the first-stage evaporator is a unipolar continuous-flow evaporator, which heats the oil-containing agent mixture to 50 degrees Celsius, evaporates to make the agent content of the mixture 40%, and the chemical vapor enters the condensing device.
  • the mixed liquid in the first-stage evaporator is pumped into the 2-stage evaporator, and the mixture of the oil-containing agent is heated to 70 degrees Celsius, and the content of the agent in the mixed solution is ⁇ 1%, and the vapor of the medicament enters the condensing device.
  • the reactor and the dry desolventizer are connected to a condensing device, and the chemical vapor in the device enters the condensing device to recover the agent.
  • the condensing unit includes a two-stage condensing process, the first-stage condensing process uses a circulating water cooling device, the condensing temperature is 20 degrees Celsius, the solvent recovery rate is >94%, the second-stage condensing process is an air chilling device, the condensing temperature is 5 degrees Celsius, and after condensation The recovery of the agent is >97%, and the condensed recovered agent can be recycled to the reactor again by the pump.
  • the diesel-based mud obtained after evaporation of the separation agent has a solid content of 10%, a maximum solid phase particle size of about 55 um, and a median particle size of about 12um, mud viscosity 56s, to achieve the technical indicators of the configuration of diesel-based mud.
  • the oil content is ⁇ 0.3%
  • the diesel-based mud recovery rate is 99.7%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, equipment investment and operation cost are low, and significant environmental benefits are obtained. , social and economic benefits.
  • This embodiment is located in an oil-based mud drilling project of an oilfield in Xinjiang.
  • the oil-based mud used is white oil-based mud, and the drilling formation is mudstone. Small, the mechanical strength of the pellet is low, and it is easy to be broken during the centrifugation process.
  • the designed processing scale is 3.0m 3 /h, and the processing capacity, treatment effect and process stability of the process are investigated.
  • the raw material is first pre-separated through a feed screen with a mesh size of 4.0 cm. After passing through the feed screen, the maximum solid particle size is 3.8 cm, the median diameter is about 0.8 mm, and the solid phase liquid content is about 16%.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • a filter screen of 1.0, 1.5, 2.0, 3.0, 4.0 mm pore size is integrated for centrifugal filtration.
  • the centrifugal speed is 700r/min.
  • the effect of centrifugal filtration with different apertures is shown in the table.
  • the filter has a pore size of 4mm, the key parameters of the process, the treatment volume reaches 3.5m 3 /h, and the liquid recovery rate reaches a maximum of 23%.
  • the phase oil content is up to 8%, so it is preferred that the filter efficiency is higher than the 4 mm aperture filter, as shown in Table 4.
  • the filtration efficiency is higher, the 4.0 mm aperture filter screen has a centrifugal speed of 600 r/min, and the material residence time in the centrifugal filtration is 6 s.
  • the coarse separation mud is transported into the buffer tank, mixed with the returned qualified mud, and homogenized, and reaches the requirement of entering the centrifugal sedimentation equipment.
  • the ratio of the coarse separation mud to the return mud is 1:1.
  • the solid content is 43%.
  • feed mud viscosity 290s.
  • the homogenized mud in the buffer tank is pumped into the centrifugal sedimentation equipment through the mud pump.
  • the on-site implementation shows that the centrifugal settling device rotates at 1800 r/min, and the drum and pusher spiral differential speed is 450 r/min.
  • the recovery rate of white oil base in oil-based drilling waste is about 61.5%
  • the solid content in white oil base is 24%
  • the maximum solid particle size is about 50um
  • the median diameter is about
  • the demulsification voltage ES is 980mV
  • the mud viscosity is 102s
  • the six-speed (3, 6, 100, 200, 300, 600r/min) results are: 6/17/58/96/142/236
  • recovery mud Reaching the reuse standard the content of pollutants in the solid phase is greatly reduced, and the petroleum content is 6%.
  • the low oil-containing solid phase adopts a desorption process at a normal temperature deep desorption process to achieve the removal of oil in the solid phase.
  • the desorbent agent in the solvent reservoir is added to the mass ratio in a ratio of 1:1.
  • the supernatant liquid is pumped into the reagent circulation subsystem, and the solid content in the liquid phase is ⁇ 15%, and the separated solid enters the solid phase desolvent reactor.
  • the oil-containing solid phase and the agent mixture in the reactor are separated, and the large-particle solids are transferred to the solid desolventizer.
  • the separated liquid phase has a solid content of ⁇ 15% and is a drug-oil-based mixture that enters the solvent circulation subsystem.
  • the evaporation device includes a 1-stage evaporator and a 2-stage evaporator.
  • the evaporation process is heated by steam, with a steam temperature of 110-125 degrees Celsius and a steam pressure of 1.1-1.2 kilograms.
  • the first-stage evaporator is a unipolar continuous-flow evaporator, heating the oil-containing agent mixture to 55 degrees Celsius, evaporating to make the agent content of the mixture 35%, and the medicament vapor enters the condensing device.
  • the mixed liquid in the first-stage evaporator is pumped into the 2-stage evaporator, and the mixture of the oil-containing agent is heated to 90 degrees Celsius, and the content of the agent in the mixed solution is ⁇ 1%, and the vapor of the medicament enters the condensing device.
  • the reactor and the dry desolventizer are connected to a condensing device, and the chemical vapor in the device enters the condensing device to recover the agent.
  • the condensing unit includes a two-stage condensing process, the first-stage condensing process uses a circulating water cooling device, the condensing temperature is 20 degrees Celsius, the solvent recovery rate is >94%, the second-stage condensing process is an air chilling device, the condensing temperature is 5 degrees Celsius, and after condensation Drug recovery rate >97%, cold
  • the condensed recovered medicament can be recycled to the reactor again by a pump.
  • the white oil base obtained after evaporation of the chemical agent has a solid content of 10%, a maximum solid phase particle size of about 55 um, a median diameter of about 12 um, and a mud viscosity of 56 s, which is a technical index for arranging the white oil-based mud.
  • the oil content is ⁇ 0.3%
  • the white oil-based mud recovery rate is 99.7%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, the equipment investment and operation cost are low, and the environment is remarkable. Benefits, social benefits and economic benefits.
  • This embodiment is located in the oil-based mud drilling project of an oilfield in Xinjiang.
  • the oil-based mud used is synthetic-based mud, and the drilling stratum is sandstone.
  • the designed and approved treatment scale is 1.5m. 3 / h, to examine the processing capacity, treatment effect and process stability of the process.
  • the raw material is first pre-separated through a feed screen.
  • the mesh size is 4 cm.
  • the solid phase After passing through the feed screen, the solid phase has a maximum particle size of 3.8 cm, a median diameter of about 0.6 mm, and a solid phase liquid content of about 16 cm. %.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • a filter screen of 1.0 mm, 1.5 mm, 2.0 mm, 3.0 mm, and 4.0 mm aperture is integrated for centrifugal filtration, and the centrifugal speed is 700 r/min, as shown in Table 7.
  • the filter efficiency is higher than a 3 mm aperture filter.
  • the filtration efficiency is higher, the 3.0 mm aperture filter screen has a centrifugal speed of 700 r/min, and the material residence time in the centrifugal filtration is 6 s.
  • the coarse separation mud is transported into the buffer tank, mixed with the returned qualified mud, and homogenized, and reaches the requirement of entering the centrifugal sedimentation equipment.
  • the ratio of the coarse separation mud to the return mud is 1:1.
  • the solid content is 35%.
  • feed mud viscosity 280s.
  • Table 9 The treatment effect of the centrifugal sedimentation equipment under different speed conditions is shown in Table 9.
  • the homogenized mud in the buffer tank is pumped into the centrifugal sedimentation equipment through the mud pump, taking into account the recovery of the mud and the quality of the recovered mud.
  • the on-site implementation shows that the centrifugal settling device rotates at 1200r/min, and the drum and pusher spiral differential are 450r/min, the ratio of the length of the settling section to the length of the compression section in the centrifugal sedimentation process is 2.5:1.
  • the disposal amount of waste oil-based mud is 2.1m 3 /h
  • the recovery rate of synthetic base oil-based mud is about 62%
  • the solid content of synthetic base oil base is 26%
  • the maximum solid-phase particle size is about 50um
  • the median diameter is About 10um
  • the demulsification voltage ES is 820mV
  • the mud viscosity is 129s
  • the six-speed (3, 6, 100, 200, 300, 600r/min) results are: 8/24/72/118/169/324, recycling
  • the mud reached the reuse standard, and the content of pollutants in the solid phase was greatly reduced, and the petroleum content was 7%.
  • the low oil-containing solid phase is subjected to a desorption process at a normal temperature and deep desorption process to achieve the removal of the oil in the solid phase.
  • the desorbent agent is added to the desorption unit in a ratio of 1:1 according to the mass ratio.
  • the supernatant is pumped into the reagent circulation subsystem, the solid content in the liquid phase is ⁇ 15%, and the residence time in the desorption reactor is 8 min, and the solid is separated into the solid phase desolvent reactor.
  • the oil-containing solid phase and the chemical mixture in the desorption reactor are separated by sedimentation, and the large-particle solid is transported to the solid desolventizer; the solid content in the separated liquid phase is ⁇ 15%, which is a medicament - Oil-based mixture, entering the solvent circulation subsystem.
  • the evaporation device includes a 1-stage evaporator and a 2-stage evaporator.
  • the evaporation process is heated by steam, with a steam temperature of 110-125 degrees Celsius and a steam pressure of 1.1-1.2 kilograms.
  • the first-stage evaporator is a unipolar continuous-flow evaporator, heating the oil-containing agent mixture to 55 degrees Celsius, evaporating to make the agent content of the mixture 35%, and the medicament vapor enters the condensing device.
  • the mixed liquid in the first-stage evaporator is pumped into the 2-stage evaporator, and the mixture of the oil-containing agent is heated to 90 degrees Celsius, and the content of the agent in the mixed solution is ⁇ 1%, and the vapor of the medicament enters the condensing device.
  • the reactor and the drying and desolventizing machine are connected to the condensing device, and the chemical vapor in the device enters the condensing device to recover the agent;
  • the condensing unit includes a two-stage condensing process, the first-stage condensing process uses a circulating water cooling device, the condensing temperature is 20 degrees Celsius, the solvent recovery rate is >94%, the second-stage condensing process is an air chilling device, the condensing temperature is 5 degrees Celsius, and after condensation The recovery of the agent is >97%, and the condensed recovered agent can be recycled to the reactor again by the pump.
  • the synthetic base oil-based mud obtained after evaporation of the separation agent has a solid content of 10%, a maximum solid phase particle size of about 55 um, a median diameter of about 12 um, and a mud viscosity of 56 s, which is a technical index for the configuration of the synthetic base oil-based mud. .
  • the oil content in the final solid phase is ⁇ 0.3%
  • the recovery rate of the synthetic base oil-based mud is 99.7%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, the equipment investment and operation cost are low, and the significant Environmental, social and economic benefits.
  • This embodiment is located in the oil-based mud drilling project of an oilfield in Xinjiang.
  • the design verification treatment scale is 2.0m 3 /h, and the processing capacity and treatment of the process are investigated. Effect and process stability.
  • the raw material is first pre-separated through a feed screen with a mesh pore size of 2.5 cm. After passing through the feed screen, the solid phase has a maximum particle size of 2.0 cm, a median diameter of about 0.6 mm, and a solid phase liquid content of about 0.6 mm. 18%.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • a filter screen of 1.0, 1.5, 2.0, 3.0, 4.0 mm pore size is integrated for centrifugal filtration.
  • the centrifugal speed was 700 r/min, and the effect of centrifugal filtration with different apertures is shown in Table 10.
  • the centrifugal filter mesh has a pore size of 2.0 mm, and the treatment effect is best.
  • the processing effect and system stability of different speed systems are shown in Table 11.
  • the filtration efficiency is higher, the 2.0 mm aperture filter screen has a centrifugal speed of 700 r/min, and the material residence time in the centrifugal filtration is 6 s.
  • the coarse separation mud is transported into the buffer tank, mixed with the returned qualified mud, and homogenized to reach the requirement of entering the centrifugal sedimentation equipment.
  • the ratio of the coarse separation mud to the return mud is 1:1.2.
  • the solid content is 40%.
  • feed mud viscosity 272s.
  • Table 12 The treatment effect of the centrifugal sedimentation equipment under different speed conditions is shown in Table 12.
  • the homogenized mud in the buffer tank is pumped into the centrifugal sedimentation equipment through the mud pump.
  • the on-site implementation shows that the centrifugal settling device rotates at 1800 r/min, and the drum and pusher spiral differential speed is 450 r/min.
  • the recovery rate of white oil base in oil-based drilling waste is about 57%
  • the solid content in white oil base is 20%
  • the maximum solid particle size is about 52um
  • the median diameter is about 8um
  • the demulsification voltage ES is 982mV
  • the mud viscosity is 122s
  • the six-speed (3, 6, 100, 200, 300, 600r/min) results are: 12/26/67/102/152/246
  • recovery mud Reaching the reuse standard the content of pollutants in the solid phase is greatly reduced, and the petroleum content is 9%.
  • the low oil-containing solid phase realizes the removal of the oil in the solid phase by the deep desorption process.
  • the solvent is added in a ratio of 1:1.2 according to the mass ratio, and the top of the solvent desorber is placed in the desorber to desorb the oil base. Mud or drill cuttings, the desorber uses a stirrer to thoroughly mix the oil-containing solid phase and solvent, and the desorption time is 30 min.
  • the oil-containing solid phase and solvent mixture in the desorber are filtered through a sieve, and large-particle solids with a particle size of >2 mm are transported to the dryer through a closed chain conveyor; solid particles and solvent-oil having a particle size of ⁇ 2 mm
  • the mixed liquid is sent together through a screw pump to the decanter centrifuge.
  • the liquid phase in the solid phase separated by the decanter centrifuge is ⁇ 20%, and is transported to the dryer through a closed chain conveyor; the solid content in the separated liquid phase is ⁇ 15%, which is a solvent-oil mixture and enters the evaporation device.
  • the evaporation process is heated by steam, with a steam temperature of 115 degrees Celsius and a steam pressure of 1.2 kilograms.
  • the solvent vapor enters the condensing unit.
  • the desorber and the dry desolventizer are connected to the condensing device, and the solvent vapor in the device enters the condensing device to recover the solvent.
  • the condensing device is a circulating water cooling device with a condensing temperature of 26 degrees Celsius and a solvent recovery of >95% after condensation.
  • the solvent recovered by condensation can be recycled to the desorber again by the pump.
  • the white oil base obtained by evaporation of the solvent has a solid content of 8%, a maximum solid phase particle size of about 55 um, a median diameter of about 10 um, and a mud viscosity of 56 s, which is a technical index for configuring the white oil-based mud.
  • the oil content in the final solid phase is 0.8%
  • the recovery rate of white oil base is 94%
  • the solvent loss is 1.5%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, equipment investment and operation cost are low, Significant environmental, social and economic benefits.
  • This embodiment is located in the oil-based mud drilling project of a certain oilfield in Xinjiang.
  • the design verification treatment scale is 2.5m 3 /h, and the treatment capacity and treatment effect of the process are investigated. And process stability.
  • the raw material is first pre-separated by a feed screen having a pore size of 3.0 cm. After passing through the feed screen, the solid phase has a maximum particle diameter of 2.0 cm, a median diameter of about 0.8 mm, and a solid phase liquid content of about 0.8 mm. 16%.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • a filter screen with a pore size of 1.5, 2.0, 3.0, and 4.0 mm is integrated for centrifugal filtration.
  • the rotation speed is 1000r/min, and the effect of centrifugal filtration with different apertures is as shown in the above 13th.
  • the centrifugal filter mesh has a pore size of 3.0 mm, and the treatment effect is best.
  • the processing effect and system stability of different speed systems are shown in Table 14.
  • the filtration efficiency is higher, the 3.0 mm aperture filter screen has a centrifugal speed of 1000 r/min, and the material residence time in the centrifugal filtration is 7 s.
  • the coarse separation mud is transported into the buffer tank, mixed with the returned qualified mud, and homogenized, and reaches the requirement of entering the centrifugal sedimentation equipment.
  • the ratio of the coarse separation mud to the return mud is 1:1.
  • the solid content is 41%.
  • feed mud viscosity 281s.
  • Table 15 The treatment effect of the centrifugal sedimentation equipment under different speed conditions is shown in Table 15.
  • the homogenized mud in the buffer tank is pumped into the centrifugal sedimentation equipment through the mud pump.
  • the on-site implementation shows that the centrifugal settling device rotates at 2000 r/min, and the drum and pusher spiral differential speed is 450 r/min.
  • the results show that after two-stage separation, the recovery rate of synthetic base in oil-based drilling waste is about 58%, the solid content in the synthetic base is 17%, the maximum solid-phase particle size is about 50um, and the median diameter is about 10um.
  • the demulsification voltage ES is 1006mV
  • the mud viscosity is 114s
  • the six-speed (3, 6, 100, 200, 300, 600r/min) results are: 16/32/88/116/172/268
  • the recovered mud reaches back.
  • the standard the content of pollutants in the solid phase is greatly reduced, and the petroleum content is 9%.
  • the low oil-containing solid phase realizes the removal of the oil in the solid phase by the desorption process.
  • the solvent is added in a ratio of 1:0.9 according to the mass ratio, and the solvent is deeply desorbed to the top of the reactor and placed in the deep desorption reactor.
  • the deep desorption reactor uses a stirrer to thoroughly mix the oil-containing solid phase and solvent, and the desorption time is 30 min.
  • the oil-containing solid phase and solvent mixture in the deep desorption reactor are filtered through a sieve, and large-particle solids with a particle size of >2 mm are transported to the dryer through a closed chain conveyor; solid particles and solvent having a particle size of ⁇ 2 mm -
  • the oil mixture is delivered together via a screw pump to the decanter centrifuge.
  • the liquid phase in the solid phase separated by the decanter centrifuge is ⁇ 20%, and is transported to the dryer through a closed chain conveyor;
  • the solid content is ⁇ 15%, which is a solvent-oil mixture and enters the evaporation device.
  • the evaporation process is heated by steam, the steam temperature is 125 degrees Celsius, the steam pressure is 4 kilograms, and the solvent vapor enters the condensing unit.
  • the deep desorption reactor and the dry desolventizer are connected to the condensing device, and the solvent vapor in the device enters the condensing device to recover the solvent.
  • the condensing device is a circulating water cooling device with a condensation temperature of 20 degrees Celsius and a solvent recovery rate of >96% after condensation.
  • the solvent recovered by condensation can be recycled to the deep desorption reactor by the pump.
  • the synthetic base obtained after evaporation of the solvent has a solid content of 8%, a maximum solid phase particle diameter of about 50 ⁇ m, a median diameter of about 10 ⁇ m, and a mud viscosity of 50 s, which is a technical index for the configuration of the synthetic base mud.
  • the oil content is 0.8%
  • the recovery rate of the synthetic base is 94%
  • the solvent loss is 1.5%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, equipment investment and operation cost are low, and significant Environmental, social and economic benefits.
  • This embodiment is located in the oil-based mud drilling project of an oilfield in Xinjiang.
  • the design verification treatment scale is 2.0m 3 /h, and the processing capacity and treatment of the process are investigated. Effect and process stability.
  • the raw material is first pre-separated through a feed screen with a mesh pore size of 3.5 cm. After passing through the feed screen, the maximum solid particle size is 2.4 cm, the median diameter is about 1.1 mm, and the solid phase liquid content is about 15%.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • a filter screen with a pore size of 1.5, 2.0, 3.0, and 4.0 mm is integrated for centrifugal filtration.
  • the centrifugal rotation speed is 1000r/min, and the effect of centrifugal filtration of different apertures is as shown in Table 16 above.
  • the treatment effect is best when the centrifugal filter screen has a pore size of 3.0 mm.
  • the treatment effect and system stability of the different speed systems are as shown in Table 17 above. Show
  • the filtration efficiency is higher, the 3.0 mm aperture filter screen has a centrifugal speed of 1000 r/min, and the material residence time in the centrifugal filtration is 6 s.
  • the coarse separation mud is transported into the buffer tank, mixed with the returned qualified mud, and homogenized, and reaches the requirement of entering the centrifugal sedimentation equipment.
  • the ratio of the coarse separation mud to the return mud is 1:1.
  • the solid content is 42%.
  • feed mud viscosity 266s.
  • Table 18 The treatment effect of the centrifugal sedimentation equipment under different speed conditions is shown in Table 18.
  • the homogenized mud in the buffer tank is pumped into the centrifugal sedimentation equipment through the mud pump.
  • the on-site implementation shows that the centrifugal settling device rotates at 1500 r/min, and the drum and pusher spiral differential speed is 450 r/min.
  • the low oil-containing solid phase realizes the removal of the oil in the solid phase by the desorption process.
  • the solvent is added in a ratio of 1:1 according to the mass ratio, and the solvent is deeply desorbed from the top of the reactor into the deep desorption reactor.
  • the deep desorption reactor uses a stirrer to thoroughly mix the oil-containing solid phase and solvent, and the desorption time is 15 min.
  • the oil-containing solid phase and solvent mixture in the deep desorption reactor are filtered through a sieve, and large-particle solids with a particle size of >2 mm are transported to the dryer through a closed chain conveyor; solid particles and solvent having a particle size of ⁇ 2 mm -
  • the oil mixture is delivered together via a screw pump to the decanter centrifuge.
  • the liquid phase in the solid phase separated by the decanter centrifuge is ⁇ 20%, and is transported to the dryer through a closed chain conveyor; the solid content in the separated liquid phase is ⁇ 15%, which is a solvent-oil mixture and enters the evaporation device.
  • the evaporation process is heated by steam, with a steam temperature of 120 degrees Celsius and a steam pressure of 1.6 kilograms.
  • the solvent vapor enters the condensing unit.
  • the deep desorption reactor and the dry desolventizer are connected to the condensing device, and the solvent vapor in the device enters the condensing device to recover the solvent.
  • the condensing device is a circulating water cooling device with a condensation temperature of 20 degrees Celsius and a solvent recovery rate of >96% after condensation.
  • the solvent recovered by condensation can be recycled to the deep desorption reactor by the pump.
  • the bio-oil base obtained by evaporation of the solvent has a solid content of 8%, a maximum solid-phase particle size of about 50 ⁇ m, and a median diameter of about 10 ⁇ m.
  • the viscosity of the mud is 50s, which is the technical index for the configuration of bio-oil-based mud.
  • the oil content in the final solid phase is 0.8%
  • the recovery rate of bio-oil base is 94%
  • the solvent loss is 1.5%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, equipment investment and operation cost are low, Significant environmental, social and economic benefits.
  • This embodiment is located in the oil-based mud drilling project of a certain oilfield in Xinjiang.
  • the design verification treatment scale is 2.2m 3 /h, and the processing capacity and treatment of the process are investigated. Effect and process stability.
  • the raw material is first pre-separated by a feed screen having a pore size of 3.0 cm. After passing through the feed screen, the maximum solid particle size is 2.0 cm, the median diameter is about 0.7 mm, and the solid phase liquid content is about 16%.
  • the pre-separated raw material enters the centrifugal separation system, and the centrifugal separation process is a coupling of the centrifugal filtration and the centrifugal sedimentation process.
  • a filter screen with a pore size of 1.5, 2.0, 3.0, and 4.0 mm is integrated for centrifugal filtration.
  • the centrifugal rotation speed was 1000 r/min, and the effect of centrifugal filtration of different apertures is shown in Table 19.
  • the centrifugal filter mesh has a pore size of 2.0 mm, and the treatment effect is best.
  • the treatment effect and system stability of different speed systems are shown in Table 20. Show.
  • the filtration efficiency is higher, the 2.0 mm aperture filter screen has a centrifugal speed of 1000 r/min, and the material residence time in the centrifugal filtration is 6 s.
  • the coarse separation mud is transported into the buffer tank, mixed with the returned qualified mud, and homogenized to reach the requirement of entering the centrifugal sedimentation equipment.
  • the ratio of the coarse separation mud to the return mud is 1:1.
  • the solid content is 34%.
  • feed mud viscosity 213s.
  • the treatment effect of the centrifugal sedimentation equipment is shown in Table 21.
  • the homogenized mud in the buffer tank is pumped into the centrifugal sedimentation equipment through the mud pump.
  • the on-site implementation shows that the centrifugal settling device rotates at 1500 r/min, and the drum and pusher spiral differential speed is 450 r/min.
  • the recovery rate of mineral oil base in oil-based drilling waste is about 56%
  • the solid content in mineral oil base is 21%
  • the maximum solid-phase particle size is about 50um
  • the median particle size is about
  • the demulsification voltage ES is 916mV
  • the mud viscosity is 134s
  • the six-speed (3, 6, 100, 200, 300, 600r/min) results are: 26/64/98/145/188/284
  • recovery mud Reaching the reuse standard the content of pollutants in the solid phase is greatly reduced
  • the petroleum content is 9%.
  • the low oil-containing solid phase realizes the removal of the oil in the solid phase by the desorption process.
  • the solvent is added in a ratio of 1:1 according to the mass ratio, and the solvent is deeply desorbed from the top of the reactor into the deep desorption reactor.
  • the deep desorption reactor uses a stirrer to thoroughly mix the oil-containing solid phase and solvent, and the desorption time is 30 min.
  • the oil-containing solid phase and solvent mixture in the deep desorption reactor are filtered through a sieve, and large-particle solids with a particle size of >2 mm are transported to the dryer through a closed chain conveyor; solid particles and solvent having a particle size of ⁇ 2 mm -
  • the oil mixture is delivered together via a screw pump to the decanter centrifuge.
  • the liquid phase in the solid phase separated by the decanter centrifuge is ⁇ 20%, and is transported to the dryer through a closed chain conveyor; the solid content in the separated liquid phase is ⁇ 15%, which is a solvent-oil mixture and enters the evaporation device.
  • the evaporation process is heated by steam, with a steam temperature of 116 degrees Celsius and a steam pressure of 1.4 kilograms.
  • the solvent vapor enters the condensing unit.
  • the deep desorption reactor and the dry desolventizer are connected to the condensing device, and the solvent vapor in the device enters the condensing device to recover the solvent.
  • the condensing device is a circulating water cooling device with a condensation temperature of 40 degrees Celsius and a solvent recovery rate of >95% after condensation.
  • the solvent recovered by condensation can be recycled to the deep desorption reactor by the pump.
  • the mineral oil base obtained by evaporation and separation of the solvent has a solid content of 8%, a maximum solid phase particle diameter of about 50 ⁇ m, a median diameter of about 10 ⁇ m, and a mud viscosity of 50 s, which is a technical index for configuring the mineral oil-based mud.
  • the oil content in the final solid phase is 0.8%
  • the recovery rate of mineral oil base is 94%
  • the solvent loss is 1.5%
  • the treatment process is carried out under normal temperature and pressure, the treatment time is short, equipment investment and operation cost are low, Significant environmental, social and economic benefits.
  • the invention is not limited to the specific embodiments described above. The invention extends to any new feature or any new combination disclosed in this specification, as well as any new method or process step or any new combination disclosed.

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Abstract

Cette invention concerne un système de recyclage de la totalité de la boue à base d'huile à partir de déchets de forage sous forme de boue à base d'huile. Lesdits déchets de forage sous forme de boue à base d'huile comprennent des débris rocheux à base d'huile, des fuites de boue de tamis vibrant, un mélange de boues de retour de cimentation de puits, des déchets boueux de retour d'arrêt de fuite, des boues de fond de complétion de puits et de nettoyage de réservoir, des eaux usées contenant de la boue à base d'huile et tous types de déchets à base d'huile pollués par de la boue à base d'huile générée au cours d'un procédé de forage à la boue à base d'huile. Ledit système de recyclage de boue à base d'huile comprend un sous-système de centrifugation à effets multiples conçu pour recycler la boue à base d'huile et un sous-système de désorption en profondeur à température normale. Le taux de recyclage de la boue à base d'huile ainsi traitée atteint 99,7%, le coût de la boue à base d'huile pour un puits unique est réduit de 8 à 10%, la teneur en huile de la phase solide finale après le traitement est inférieure à 0,3% et les normes de protection de l'environnement sont respectées. Le système selon l'invention résout le problème technique du recyclage rapide et de l'utilisation cyclique de la boue à base d'huile, qui est un produit onéreux, dans tous types de déchets à base d'huile générés lors d'un procédé de forage de puits. Ledit système assure en outre une réelle protection de l'environnement au cours du procédé de traitement sans entraîner de pollution secondaire de telle sorte que la performance de la boue à base d'huile recyclée est conforme aux normes de recyclage.
PCT/CN2014/093078 2013-12-05 2014-12-05 Système de recyclage de la totalité de la boue à base d'huile à partir de déchets de forage sous forme de boue à base d'huile WO2015081878A1 (fr)

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CN2013106442006 2013-12-05
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CN201320789889 2013-12-05
CN201310644199 2013-12-05
CN201320791340.1U CN203741273U (zh) 2013-12-05 2013-12-05 废弃油基钻井废物中基油回收的药剂常温深度脱附反应器
CN201310644198 2013-12-05
CN2013207898897 2013-12-05
CN201310645168.3A CN103643910B (zh) 2013-12-05 2013-12-05 一种废弃油基泥浆中泥浆及柴油基的回收装备
CN2013106441982 2013-12-05
CN2013207911891 2013-12-05
CN201320791189.1U CN203669849U (zh) 2013-12-05 2013-12-05 一种油基钻井含油废物中油基泥浆回收装置
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CN113530505A (zh) * 2020-04-22 2021-10-22 中国石油天然气股份有限公司 一种高凝油油泥调剖地面注入加热保温系统及方法
CN114409210A (zh) * 2022-02-18 2022-04-29 湖北中油科昊机械制造有限公司 一种混合均匀的可监测式油基泥浆处理装置
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CN106968629B (zh) * 2016-01-14 2023-09-08 中石化石油工程技术服务有限公司 一种全井段钻屑及废弃钻井液不落地处理装备
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CN106194078B (zh) * 2016-07-19 2020-07-17 大庆乾晟润水江环保科技有限公司 钻井泥浆不落地处理装置
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CN106930727A (zh) * 2017-05-05 2017-07-07 成都大有石油钻采工程有限公司 一种适用于钻井清洁生产废弃物随钻不落地处理的装置及方法
CN107489385A (zh) * 2017-08-17 2017-12-19 黑龙江省万意达石油工程有限公司 撬装式钻井油基、水基泥浆不落地处理环保系统及其处理工艺
CN107489385B (zh) * 2017-08-17 2023-10-17 黑龙江省万意达石油工程有限公司 撬装式钻井油基、水基泥浆不落地处理环保系统
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CN110080701A (zh) * 2018-01-26 2019-08-02 中石化石油工程技术服务有限公司 一种钻屑随钻生物处理系统
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CN109488238B (zh) * 2019-01-18 2023-09-19 北京探矿工程研究所 一种地质钻探多功能一体化钻井液综合处理系统及处理方法
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WO2021061086A1 (fr) * 2019-09-23 2021-04-01 Ally Onsite Système de gestion de solides et de liquides et appareils pour le forage de puits de pétrole et de gaz
US11643888B2 (en) 2019-09-23 2023-05-09 Innovative Solutions, Ltd. Solids and liquids management system and apparatus for oil and gas well drilling
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CN115506735A (zh) * 2021-06-07 2022-12-23 中国石油化工股份有限公司 一种钻井液回收利用系统
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CN115068984A (zh) * 2022-03-09 2022-09-20 山东明化新材料有限公司 一种树脂生产有机溶剂中高聚物的分离回收系统
CN115044387A (zh) * 2022-06-27 2022-09-13 重庆瀚渝再生资源有限公司 油基岩屑处理系统及工艺
CN115044387B (zh) * 2022-06-27 2024-01-23 重庆瀚渝再生资源有限公司 油基岩屑处理系统及工艺
CN115784546B (zh) * 2023-02-07 2023-04-07 佛山市铁人环保科技有限公司 一种石油重金属复合污染泥浆的处置方法
CN115784546A (zh) * 2023-02-07 2023-03-14 佛山市铁人环保科技有限公司 一种石油重金属复合污染泥浆的处置方法

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