CN103773408B - One reclaims oil-base mud and oil base technique from oil-base mud drilling wastes - Google Patents
One reclaims oil-base mud and oil base technique from oil-base mud drilling wastes Download PDFInfo
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Abstract
The invention belongs to the process field of oil-base mud or oil-based drill cuttings in shale gas, tight gas and the drilling well of conventional gas and oil field, particularly relate to synchronous recovery oil-base mud and oil base process recovery process in a kind of oil-base mud drilling wastes.It is characterized in that: described process recovery process comprises oil-base mud centrifugal separation processes, medicament normal-temperature deep desorption reclaims oil base sludge process and oil-containing medicament mixing distillation-condensation medicament reuse process.Reaction process in the present invention can either realize the harmless treatment of oil-base mud or drilling cuttings, the oleaginousness & lt in final solid formation; 1%, the most of oil content in oil-base mud or drilling cuttings can be reclaimed again, the rate of recovery & gt of oil base; 90%, the pharmacy response used almost can reclaim completely and reuse, drug out loss & lt; 2%, and treating processes is carried out all at normal temperatures and pressures, and the treatment time is short, and almost second time is not polluted, and facility investment and running cost are all lower, have significant environmental benefit, Social benefit and economic benefit.
Description
Technical field
The invention belongs to the process field of oil-base mud or oil-based drill cuttings in shale gas, tight gas and the drilling well of conventional gas and oil field, particularly relate to synchronous recovery oil-base mud and oil base process recovery process in a kind of oil-base mud drilling wastes.
Background technology
In the drilling engineering of salt deposit, sound plaster, carnallite layer and high temperature deep well, the use of oil-base mud is increasingly extensive, in drilling process, mixes the drilling wastes that slurry is representative by producing with waste drilling mud, mud tank bed mud, well cementation.This type of waste is a kind of complicated heterogeneous system containing mineral oil, phenolic compound and heavy metal, principal pollutant come from the oil base of oil-base mud, and drilling well oil base conventional at present comprises diesel oil based, white oil base, biological oil base, mineral oil based, synthetic oil-base etc.Aromatic hydrocarbon in diesel oil has larger bio-toxicity, if effectively do not processed and will cause great effect to region environment.Oily waste is also the HW08 class danger wastes demarcated in country's " danger wastes register " simultaneously.According to environmental requirement, discarded oil-base mud and oil-base mud drilling cuttings all will carry out post-processed.Process oil-base mud or drilling cuttings mode traditionally and have burning disposal, cracking process, biological degradation etc., but burning method infusion of financial resources is large, running cost is high, the waste gas that simultaneously produces in burning process easily causes second time environmental pollution; For the oil-contained drilling cuttings that part oleaginousness is lower, adopt land-fill method process, landfill method investment is less, but it does not really eliminate oil pollutant in oil-contained drilling cuttings, rainy season shower, and the infiltration of underground water likely causes oil base to overflow, Polluted area environment; Biochemical process is also one of mode commonly used at present, adopt its cost of petroleum hydrocarbons in the Degradation process oil-contained drilling cuttings of microorganism lower, but treatment cycle is longer, and the arene in oil base has certain toxicity, likely suppresses biochemical degradation process.Oil base in discarded oil-base mud as refuse process, is not realized the resource utilization reuse of oil base by this type of technique.
Summary of the invention
For solving above technical problem, the invention provides a kind of cost low, do not bring second time to pollute and recyclable resource operation is simple a kind of from oil-containing drilling wastes, reclaim oil-base mud and oil base technique.Described oil-base mud drill waste comprises diesel oil based, white oil base, biological oil base, mineral oil based and synthesis base and discards the oil-containing drill waste such as oil-based drilling mud, mud tank bed mud, the mixed slurry of well cementation and oil-contained drilling cuttings.
The one solving above technical problem reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: described process recovery process comprises oil-base mud centrifugal separation processes, medicament normal-temperature deep desorption reclaims oil base sludge process and oil-containing medicament mixing distillation-condensation medicament reuse process.
Process recovery process described in the present invention and also comprise charging roughing out technique.The stone of greater particle size easily causes the blocking of feed port, and charging, by reflux, causes treatment effect poor.Adopt vibratory screening apparatus to carry out roughing out to fill process, mesh size is 2 ~ 3cm, and vibrational frequency is 180 ~ 200r/min, screen area 1 ~ 1.5m2/m3.
Oil-base mud centrifugal separation processes of the present invention, realizes the recovery of oil-base mud by centrifuging and centrifugal settling coupling process.Isolated liquid phase reaches the qualified oil-base mud of drilling engineering reuse requirement, and isolated solid phase oil length is lower, and grain diameter is comparatively large, is conducive to the enforcement that follow-up normal-temperature deep desorption reclaims oil base technique.
In described centrifuging, rotary drum rotating speed is 400 ~ 3000r/min.
In described centrifuging, filtering net aperture is 0.5-4.0mm.
In described centrifuging, residence time of material is 6 ~ 8s.
After described centrifuging, the roughing out mud solid content of gained is high, and sand content is large, and viscosity is large, does not reach oil-base mud reuse performance index, needs to adopt centrifugal settling unit to be further processed roughing out mud.
Described centrifugal settling process, after roughing out mud enters centrifugal settling equipment rotary drum, rotary drum high-speed rotation, solid phase particles rapid subsidence larger than density of liquid phase under the powerful centrifugal action of rotary drum is to drum inner wall, by spiral conveyer, the solid phase being deposited on drum inner wall is pushed to the compression section of rotary drum small end, carry out compressing de-liquid, then discharge through slag notch, the qualified mud after separation then flows out from the large end overflow weir of rotary drum.
In described centrifugal settling, rotary drum rotating speed is 600-3000r/min, and rotary drum and pushing spiral differential are <300r/min, the preferred 1200-2100r/min of rotary drum rotating speed,
Have homogenizing process between described centrifuging, centrifugal settling process, the roughing out mud that namely centrifugal filter is produced pumps into homogenization buffer tank.Homogenization buffer tank plays the effect of buffering, homogeneous, the roughing out mud that centrifugal filter is produced is carried out with the qualified mud that centrifugal settling is produced mix, homogeneous, after reaching the charging standard entering horizontal screw centrifuge, pump into horizontal screw centrifuge and carry out centrifugal settling separation.After the mud that horizontal screw centrifuge is separated reaches reuse standard, part enters possum belly, and part gets back to homogeneous tank;
To adopt in the present invention after centrifuging and the process of centrifugal settling two-stage centrifugal process recovery process, the oil-base mud rate of recovery can reach 70%, reclaim oil-base mud solid content 10 ~ 20%, maximum solid phase particle diameter is about 50 ~ 80um, median particle diameter is about 10 ~ 30um, emulsion-breaking voltage ES is 700 ~ 2000mV mud viscosity, 100 ~ 150s, six speed (3, 6, 100, 200, 300, measurement result 600r/min) is: (6 ~ 10)/(12 ~ 40)/(50 ~ 80)/(90 ~ 120)/(130 ~ 180)/(240 ~ 400), the oil-base mud reclaimed can reclaim new opplication of laying equal stress in drilling engineering.The solid formation petroleum class content <8% be separated.
The low oil-containing solid phase normal-temperature deep desorption that technique of the present invention produces after also comprising centrifugation reclaims the evaporation-condensation reuse operation of oil base operation and medicament.
Described medicament normal-temperature deep desorption be by medicament according to mass ratio with 0.7/1 ~ 1/1 ratio add, medicament puts into reactor from reactor head, normal-temperature deep desorption is utilized to realize oil, the mud separation of solid phase surface, adopt agitator that oil-containing solid phase and medicament are fully mixed, reaction times 10 ~ 30min.
In described medicament normal-temperature deep separating process, in reactor, oil-containing solid phase and pharmaceutical mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by solid-handling equipment; The solid particulate of particle diameter <2mm and medicament-oily mixed solution are together transported to solid-liquid separating equipment by spiral pump, and the solid phase after separation is transported to moisture eliminator by solid-handling equipment, and liquid phase is medicament-oily mixed solution, enters evaporation unit.
After described solid-liquid separation process, liquid holdup <20% in solid phase, solid content <15% in liquid phase.
Described evaporation unit comprises 1 grade of vaporizer and 2 grades of vaporizers.Evaporative process utilizes steam heating, vapor temperature 110 ~ 125 DEG C, vapor pressure 1 ~ 4 kilogram.
Described 1 grade of vaporizer is one pole Continuous Flow vaporizer, and heating oil-containing medicament mixed solution is to 50 ~ 60 DEG C, and evaporation makes mixed solution Chinese medicine content <40%, and medicament steam enters condensing equipment.
Described 2 grades of vaporizers are two intermittent type vaporizers in parallel, and heating oil-containing medicament mixed solution is to 70 ~ 90 DEG C, and evaporation makes mixed solution Chinese medicine content <0.5%, and medicament steam enters condensing equipment.
Described condensing equipment can be circulating water cooling device, air cooling apparatus or vaporizer-condenser, condensing temperature 20 ~ 40 degrees Celsius, medicament rate of recovery >95% after condensation, and the medicament that condensation is reclaimed loops back reactor again by pump.
Described reactor head can be connected with condensing equipment, and the nitrogen passed into enters condensing equipment, and the medicament steam of stripping is reclaimed in condensation, can by reaction process and the medicament of a small amount of gasification reclaim.
Moisture eliminator top is connected with condensing equipment, and the medicament steam produced in drying process enters condensing equipment, and the medicament steam produced in drying process is reclaimed in condensation.
Be separated in the oil base obtained after medicament through pervaporation, solid content <10%, maximum solid phase particle diameter is about 50 ~ 80um, and median particle diameter is about 10 ~ 30um, liquid viscosity <60s, reaches the technical indicator of configuration oil-base mud.
Reaction process in the present invention can either realize the harmless treatment of oil-base mud or drilling cuttings, oleaginousness <1% in final solid formation, the most of oil content in oil-base mud or drilling cuttings can be reclaimed again, the rate of recovery >90% of oil base, the pharmacy response used almost can reclaim completely and reuse, drug out loss <2%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, almost second time is not polluted, facility investment and running cost are all lower, there is significant environmental benefit, Social benefit and economic benefit.
From high oil-containing drilling wastes, synchronously oil-base mud and oil base can be reclaimed in the present invention.
Accompanying drawing explanation
Fig. 1 is the process flow sheet in the present invention in embodiment.
Embodiment
The process recovery process of a kind of oil-base mud or drilling cuttings in the present invention, is characterized in that: described process recovery process comprises centrifugation, medicament normal-temperature deep desorption and distillation condensation, and process recycled by medicament.Its operation scheme feature is that the foreign matters such as opening for feed is connected with vibratory screening apparatus, the stone on vibratory screening apparatus top enter reactor by handling machinery, is transported to moisture eliminator after completing medicament normal-temperature deep desorption workshop section; Vibratory screening apparatus lower liquid phase mud enters centrifugal filter and carries out centrifuging.The solid phase that centrifuging completes generation is transported to reactor by handling machinery, is transported to moisture eliminator after completing medicament normal-temperature deep desorption workshop section; The roughing out mud that centrifugal filter is produced can pump into homogenization buffer tank.Homogenization buffer tank plays the effect of buffering, homogeneous, the roughing out mud that centrifugal filter is produced is carried out with the qualified mud that rear end produces mix, homogeneous, after reaching the charging standard entering horizontal screw centrifuge, pump into horizontal screw centrifuge and carry out centrifugal settling separation, horizontal screw centrifuge is separated solid phase and is transported to reactor by handling machinery, the liquid phase be separated is qualified mud, and part enters possum belly, and part gets back to homogeneous tank.The solid phase of vibratory screening apparatus, centrifugal filter and centrifugal settling device separates enters reactor, realize fully mixing of medicament and low oil-containing solids thing in the reactor, and carry out solid-liquid separation by inside reactor screen cloth, macrobead solid phase enters dry desolventizing machine, horizontal screw centrifuge is entered containing short grained liquid phase, solid-liquid is carried out by horizontal screw centrifuge, the solid granule be separated enters moisture eliminator drying, the liquid phase oil-containing medicament be separated enters No. 1 vaporizer and carries out initial concentration, then No. 2 vaporizers are entered, evaporated completely by medicament, the oil base of production pumps into oil base storage tank.The medicament steam that the medicament steam of No. 1 vaporizer and No. 2 vaporizer generations and dry desolventizing machine produce enters condenser, and the insecticide liquid of condensation is back to medicament storage tank, and cyclically utilizing is to conversion unit.Condenser adopts circulating cooling water cooling.No. 1 vaporizer, No. 2 vaporizers and moisture eliminator adopt steam heating.Solid-handling equipment can be spiral conveyer, chain scraper machine or airtight transport tape.Solid-liquid separating equipment can be airtight sedimentation centrifuge or closed filter press.
embodiment 1
The present embodiment is arranged in oil field, northwest oil-base mud drilling engineering, in the processing item of discarded oil-base mud and oil-contained drilling cuttings, adopts diesel oil based drilling mud; drilling stratum is sandstone; the particle diameter of drilling cuttings is less, and particle physical strength is lower, easily broken in centrifugal separation processes process.Technique comprises centrifugation, medicament reaction and distillation condensation process.Adopting design to appraise and decide treatment scale is 0.8m3/h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 3cm, and after charging screen cloth, solid phase maximum particle diameter is 2.6cm, and median particle diameter is about 1.0mm, and solid phase liquid content is about 16%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.Centrifuging adopts frequency conversion centrifugal filter to carry out centrifuging, mainly through under centrifugal action, by the interception of screen cloth, realizes being separated of macrobead drilling cuttings and oil-base mud.
In implementation process comprehensive preferably 0.5,0.8,1.5,2.0, the filter screen in 4.0mm aperture carries out centrifuging, centrifugal rotational speed is 800r/min, and it is as shown in the table for different pore size centrifuging implementation result, as aperture of filter screen 2mm, technology key index, treatment capacity reaches 0.92m
3/ h, the liquid phase rate of recovery reaches maximum value 25%, is separated solid phase oil length and reaches 6%, although solid content two indices is higher in density of liquid phase and liquid phase, but consider that subsequent technique can remove the solid formation in roughing out mud further, what therefore preferred filtration efficiency was higher is that 2mm aperture filter screen is as table 1.General centrifuging technique mainly utilizes less filtration space and forms thicker cake layer, utilizes retaining of cake layer, realizes solid-liquid separation.But discarded drilling and completing fluids is than great, and viscosity is large, adopts general centrifuging technique to have larger limitation.
Table 1
In implementation process, under the 2mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are as shown in table 2.
Table 2
Traditional centrifuging viewpoint, under higher speed conditions, liquid phase centrifugal force in rotary drum is comparatively large, is conducive to solid-liquid separation.Under simultaneously higher speed conditions, discharging revolution speed of screw is accelerated, and the residence time of material in rotary drum is shorter, and its separation efficiency is poor.It is more dry, comparatively hard that too fast rotating speed causes cake layer to be formed, and causes later stage separation efficiency poor, and the cake layer formed compared with the slow speed of revolution is comparatively loose, is conducive to the separation of liquid phase.Higher rotating speed centrifugal force is comparatively large, and be conducive to the filtration of liquid, but material is easily ground by too high rotating speed, the material be grated mixes with mud cake further, effective separate solid particles weak effect; And higher rotating speed causes spiral discharging speed to be accelerated, the residence time of material in rotary drum is shorter, and its separation efficiency is poor.It is more dry, comparatively hard that too fast rotating speed causes cake layer to be formed, and causes later stage separation efficiency poor, so comparatively loose compared with the cake layer of slow speed of revolution formation, is conducive to the separation of liquid phase.
Under the processing condition optimizing rotating speed 750r/min and aperture of filter screen 2mm, technology key index, treatment capacity reaches 0.92m
3/ h, the liquid phase rate of recovery reaches maximum value 28%, is separated solid phase oil length and reaches 6%, and the solid phase particles be simultaneously separated is comparatively large, is conducive to subsequent reactions workshop section, and system cloud gray model is steady, in quality two key parameters for the treatment of capacity and roughing out mud, obtain good balance.
After other parameters of process operation comprise centrifuging, the roughing out mud solid content of gained is about 47%, and in solid phase, maximum particle diameter is about 2.5cm, and median particle diameter is about 0.08mm, and emulsion-breaking voltage ES is 415mV, mud viscosity >500s,
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump.For the material characteristic of the discarded slurry of process in test, under testing different rotary drum speed conditions, centrifugal settling solid-liquid separation effect, as table 3.
Table 3
Field conduct shows that centrifugal settling equipment rotating speed is 2100r/min, and rotary drum and pushing spiral differential are 300r/min.Result of implementation shows after two-stage is separated, in oil base drilling wastes, the rate of recovery of diesel oil based is about 71%, solid content 14% in diesel oil based, and maximum solid phase particle diameter is about 50um, median particle diameter is about 10um, emulsion-breaking voltage ES is 1150mV mud viscosity 124s, six speed (3,6,100,200,300,600r/min) measurement result be: 8/22/70/114/168/253, reclaim mud reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 7%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by medicament normal-temperature deep separating process, the present embodiment Chinese medicine adds with the ratio of 0.7:1 according to mass ratio, medicament puts into reactor from reactor head, adopts agitator that oil-containing solid phase and medicament are fully mixed, reaction times 10min.
After having reacted, in reactor, oil-containing solid phase and pharmaceutical mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with medicament-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is medicament-oily mixed solution, enters evaporation unit.
Evaporation unit comprises 1 grade of vaporizer and 2 grades of vaporizers.Evaporative process utilizes steam heating, vapor temperature 125 degrees Celsius, vapor pressure 4 kilograms.1 grade of vaporizer is one pole Continuous Flow vaporizer, and heating oil-containing medicament mixed solution is to 50 degrees Celsius, and evaporation makes mixed solution Chinese medicine content 40%, and medicament steam enters condensing equipment.In 1 grade of vaporizer, mixed solution pumps into 2 grades of vaporizers, and heating oil-containing medicament mixed solution is to 70 degrees Celsius, and evaporation makes mixed solution Chinese medicine content <0.5%, and medicament steam enters condensing equipment.
Reactor is connected with condensing equipment with dry desolventizing machine, and the medicament steam in equipment enters condensing equipment, reclaims medicament
Condensing equipment is circulating water cooling device, condensing temperature 20 degrees Celsius, medicament rate of recovery >96% after condensation, and the medicament that condensation is reclaimed loops back reactor again by pump.
Be separated in the diesel oil based obtained after medicament through pervaporation, solid content 10%, maximum solid phase particle diameter is about 55um, and median particle diameter is about 12um, mud viscosity 56s, reaches the technical indicator of configuration diesel oil based mud.
Oleaginousness <1% in final solid formation, the rate of recovery 92% of diesel oil based, drug out loss 2%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
embodiment 2
The present embodiment is arranged in oil field, Xinjiang oil-base mud drilling engineering; in the processing item of discarded oil-base mud and oil-contained drilling cuttings; the oil-base mud adopted is diesel oil based mud; drilling stratum is mud stone; the particle diameter of drilling cuttings is less; particle physical strength is lower, and easily broken in centrifugal separation processes process, adopting design to appraise and decide treatment scale is 3.0m
3/ h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 2.8cm, and after charging screen cloth, solid phase maximum particle diameter is 2.2cm, and median particle diameter is about 0.8mm, and solid phase liquid content is about 16%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.In centrifuging process implementing process comprehensive preferably 1.0,1.5,2.0,3.0, the filter screen in 4.0mm aperture carries out centrifuging.Centrifugal rotational speed is 700r/min, and it is as shown in the table for different pore size centrifuging implementation result, and as aperture of filter screen 4mm, technology key index, treatment capacity reaches 3.5m
3/ h, the liquid phase rate of recovery reaches maximum value 23%, is separated solid phase oil length and reaches 8%, and what therefore preferred filtration efficiency was higher is 4mm aperture filter screen, as table 4.
Table 4
In implementation process, under the 4mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are as shown in table 5.
Table 5
What preferred filtration efficiency was higher is 4.0mm aperture filter screen, and centrifugal rotational speed is 600r/min, and in centrifuging, residence time of material is 6s.Roughing out slurry transportation enters in surge tank, and mix with the qualified mud of backflow, after homogeneous, reach and enter centrifugal settling equipment requirements, roughing out mud is 1:1 with the ratio of backflow mud, after mixing homogeneous, Gu containing being 43%, and feed mud viscosity, 290s.Under different rotating speeds condition, the treatment effect of centrifugal settling equipment is as shown in table 6.
Table 6
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump, and field conduct shows that centrifugal settling equipment rotating speed is 1800r/min, and rotary drum and pushing spiral differential are 450r/min.Result of implementation shows after two-stage is separated, in oil base drilling wastes, the rate of recovery of diesel oil based is about 67%, solid content 24% in diesel oil based, maximum solid phase particle diameter is about 50um, median particle diameter is about 10um, and emulsion-breaking voltage ES is 980mV, mud viscosity 102s, six speed (3,6,100,200,300,600r/min) measurement result be: 6/17/58/96/142/236, reclaim mud and reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 6%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by medicament normal-temperature deep separating process, the present embodiment Chinese medicine adds with the ratio of 1:1 according to mass ratio, medicament puts into reactor from reactor head, adopts agitator that oil-containing solid phase and medicament are fully mixed, reaction times 30min.
After having reacted, in reactor, oil-containing solid phase and pharmaceutical mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with medicament-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is medicament-oily mixed solution, enters evaporation unit.
Evaporation unit comprises 1 grade of vaporizer and 2 grades of vaporizers.Evaporative process utilizes steam heating, vapor temperature 120 degrees Celsius, vapor pressure 1.6 kilograms.1 grade of vaporizer is one pole Continuous Flow vaporizer, and heating oil-containing medicament mixed solution is to 50 degrees Celsius, and evaporation makes mixed solution Chinese medicine content 34%, and medicament steam enters condensing equipment.In 1 grade of vaporizer, mixed solution pumps into 2 grades of vaporizers, and heating oil-containing medicament mixed solution is to 85 degrees Celsius, and evaporation makes mixed solution Chinese medicine content 0.4%, and medicament steam enters condensing equipment.
Reactor is connected with condensing equipment with dry desolventizing machine, and the medicament steam in equipment enters condensing equipment, reclaims medicament
Condensing equipment is circulating water cooling device, condensing temperature 22 degrees Celsius, medicament rate of recovery >95% after condensation, and the medicament that condensation is reclaimed loops back reactor again by pump.
Be separated in the diesel oil based obtained after medicament through pervaporation, solid content 10%, maximum solid phase particle diameter is about 55um, and median particle diameter is about 12um, mud viscosity 56s, reaches the technical indicator of configuration diesel oil based mud.
Oleaginousness 0.8% in final solid formation, the rate of recovery 94% of diesel oil based, drug out loss 1.5%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
embodiment 3
The present embodiment is arranged in Xinjiang Oilfield oil-base mud drilling engineering, and in the processing item of discarded oil-base mud and oil-contained drilling cuttings, the oil-base mud of employing is diesel oil based mud, and drilling stratum is sandstone, and adopting design to appraise and decide treatment scale is 1.5m
3/ h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 2cm, and after charging screen cloth, solid phase maximum particle diameter is 1.8cm, and median particle diameter is about 0.6mm, and solid phase liquid content is about 16%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.In centrifuging process implementing process comprehensive preferably 1.0,1.5,2.0,3.0, the filter screen in 4.0mm aperture carries out centrifuging, centrifugal rotational speed is 700r/min, as table 7.
Table 7
It is as shown in the table for different pore size centrifuging implementation result, and as aperture of filter screen 3mm, technology key index, treatment capacity reaches 1.7m
3/ h, the liquid phase rate of recovery reaches maximum value 28%, is separated solid phase oil length and reaches 8%, and what therefore preferred filtration efficiency was higher is 3mm aperture filter screen.
In implementation process, under the 3mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are as shown in table 8.
Table 8
What preferred filtration efficiency was higher is 3.0mm aperture filter screen, and centrifugal rotational speed is 700r/min, and in centrifuging, residence time of material is 6s.Roughing out slurry transportation enters in surge tank, and mix with the qualified mud of backflow, after homogeneous, reach and enter centrifugal settling equipment requirements, roughing out mud is 1:1 with the ratio of backflow mud, after mixing homogeneous, Gu containing being 35%, and feed mud viscosity, 280s.Under different rotating speeds condition, the treatment effect of centrifugal settling equipment is as shown in table 9.
Table 9
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump, consider the yield of mud and reclaim the quality of mud, field conduct shows that centrifugal settling equipment rotating speed is 1200r/min, rotary drum and pushing spiral differential are 450r/min, and centrifugal settling Settlement segment length and compression section length ratio are 2.5:1.The treatment capacity of discarded oil-base mud is 2.1m
3/ h, the rate of recovery of diesel oil based mud is about 62%, solid content 26% in diesel oil based, maximum solid phase particle diameter is about 50um, and median particle diameter is about 10um, emulsion-breaking voltage ES is 820mV, mud viscosity 129s, six speed (3,6,100,200,300,600r/min) measurement result be: 8/24/72/118/169/324, reclaim mud reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 7%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by medicament normal-temperature deep separating process, the present embodiment Chinese medicine adds with the ratio of 0.8:1 according to mass ratio, medicament is put from reactor head, adopts agitator that oil-containing solid phase and medicament are fully mixed, reaction times 25min.
After having reacted, in reactor, oil-containing solid phase and pharmaceutical mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with medicament-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is medicament-oily mixed solution, enters evaporation unit.
Evaporation unit comprises 1 grade of vaporizer and 2 grades of vaporizers.Evaporative process utilizes steam heating, vapor temperature 115 degrees Celsius, vapor pressure 1.2 kilograms.1 grade of vaporizer is one pole Continuous Flow vaporizer, and heating oil-containing medicament mixed solution is to 55 degrees Celsius, and evaporation makes mixed solution Chinese medicine content 30%, and medicament steam enters condensing equipment.In 1 grade of vaporizer, mixed solution pumps into 2 grades of vaporizers, and heating oil-containing medicament mixed solution is to 88 degrees Celsius, and evaporation makes mixed solution Chinese medicine content 0.3%, and medicament steam enters condensing equipment.
Reactor is connected with condensing equipment with dry desolventizing machine, and the medicament steam in equipment enters condensing equipment, reclaims medicament
Condensing equipment is circulating water cooling device, condensing temperature 20 degrees Celsius, the medicament rate of recovery 97% after condensation, and the medicament that condensation is reclaimed loops back reactor again by pump.
Be separated in the diesel oil based obtained after medicament through pervaporation, solid content 7%, maximum solid phase particle diameter is about 50um, and median particle diameter is about 10um, mud viscosity 54s, reaches the technical indicator of configuration diesel oil based mud.
Oleaginousness 0.6% in final solid formation, the rate of recovery 96% of diesel oil based, drug out loss 1.3%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
embodiment 4
The present embodiment is arranged in oil field, Xinjiang oil-base mud drilling engineering, adopts white oil base to discard in the processing item of oil-base mud and oil-contained drilling cuttings, and adopting design to appraise and decide treatment scale is 2.0m
3/ h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 2.5cm, and after charging screen cloth, solid phase maximum particle diameter is 2.0cm, and median particle diameter is about 0.6mm, and solid phase liquid content is about 18%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.In centrifuging process implementing process comprehensive preferably 1.0,1.5,2.0,3.0, the filter screen in 4.0mm aperture carries out centrifuging.Centrifugal rotational speed is 700r/min, and different pore size centrifuging implementation result is as shown in table 10.
Table 10
Consider treatment capacity and reclaim quality of mud fluid, during centrifuging aperture of filter screen 2.0mm, treatment effect is best, and in implementation process, under the 2mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are as shown in table 11.
Table 11
What preferred filtration efficiency was higher is 2.0mm aperture filter screen, and centrifugal rotational speed is 700r/min, and in centrifuging, residence time of material is 6s.Roughing out slurry transportation enters in surge tank, and mix with the qualified mud of backflow, after homogeneous, reach and enter centrifugal settling equipment requirements, roughing out mud is 1:1.2 with the ratio of backflow mud, after mixing homogeneous, Gu containing being 40%, and feed mud viscosity, 272s.Under different rotating speeds condition, the treatment effect of centrifugal settling equipment is as shown in table 12.
Table 12
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump, and field conduct shows that centrifugal settling equipment rotating speed is 1800r/min, and rotary drum and pushing spiral differential are 450r/min.Result of implementation shows after two-stage is separated, in oil base drilling wastes, the rate of recovery of white oil base is about 57%, solid content 20% in white oil base, maximum solid phase particle diameter is about 52um, median particle diameter is about 8um, and emulsion-breaking voltage ES is 982mV, mud viscosity 122s, six speed (3,6,100,200,300,600r/min) measurement result be: 12/26/67/102/152/246, reclaim mud and reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 9%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by leaching technology, in the present embodiment, solvent adds with the ratio of 1:1.2 according to mass ratio, leacher is put at solvent leacher top, leaching oil base mud or drilling cuttings, leacher adopts agitator that oil-containing solid phase and solvent are fully mixed, leaching time 30min.
After having leached, in leacher, oil-containing solid phase and solvent mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with solvent-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is solvent-oily mixed solution, enters evaporation unit.
Evaporative process utilizes steam heating, vapor temperature 115 degrees Celsius, vapor pressure 1.2 kilograms.Solvent vapour enters condensing equipment.
Leacher is connected with condensing equipment with dry desolventizing machine, and the solvent vapo(u)r in equipment enters condensing equipment, recycling design
Condensing equipment is circulating water cooling device, condensing temperature 26 degrees Celsius, and solvent recovering rate >95% after condensation, condensation recovered solvent loops back leacher again by pump.
Be separated in the white oil base obtained after solvent through pervaporation, solid content 8%, maximum solid phase particle diameter is about 55um, and median particle diameter is about 10um, mud viscosity 56s, reaches the technical indicator configuring white oil-base mud.
Oleaginousness 0.8% in final solid formation, the rate of recovery 94% of white oil base, solvent loss 1.5%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
embodiment 5
The present embodiment is arranged in oil field, Xinjiang oil-base mud drilling engineering, and adopt synthesis base to discard in the processing item of oil-base mud and oil-contained drilling cuttings, adopting design to appraise and decide treatment scale is 2.5m
3/ h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 3.0cm, and after charging screen cloth, solid phase maximum particle diameter is 2.0cm, and median particle diameter is about 0.8mm, and solid phase liquid content is about 16%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.In centrifuging process implementing process comprehensive preferably 1.5,2.0,3.0, the filter screen in 4.0mm aperture carries out centrifuging.Centrifugal rotational speed is 1000r/min, and different pore size centrifuging implementation result is as shown in table 13.
Table 13
Consider treatment capacity and reclaim quality of mud fluid, during centrifuging aperture of filter screen 3.0mm, treatment effect is best, and in implementation process, under the 3mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are as shown in table 14.
Table 14
What preferred filtration efficiency was higher is 3.0mm aperture filter screen, and centrifugal rotational speed is 1000r/min, and in centrifuging, residence time of material is 7s.Roughing out slurry transportation enters in surge tank, and mix with the qualified mud of backflow, after homogeneous, reach and enter centrifugal settling equipment requirements, roughing out mud is 1:1 with the ratio of backflow mud, after mixing homogeneous, Gu containing being 41%, and feed mud viscosity, 281s.Under different rotating speeds condition, the treatment effect of centrifugal settling equipment is as shown in Table 15.
Table 15
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump, and field conduct shows that centrifugal settling equipment rotating speed is 2000r/min, and rotary drum and pushing spiral differential are 450r/min.Result of implementation shows after two-stage is separated, in oil base drilling wastes, the rate of recovery of synthesis base is about 58%, solid content 17% in synthesis base, maximum solid phase particle diameter is about 50um, median particle diameter is about 10um, and emulsion-breaking voltage ES is 1006mV, mud viscosity 114s, six speed (3,6,100,200,300,600r/min) measurement result be: 16/32/88/116/172/268, reclaim mud and reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 9%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by leaching technology, in the present embodiment, solvent adds with the ratio of 1:0.9 according to mass ratio, leacher is put at solvent leacher top, leaching oil base mud or drilling cuttings, leacher adopts agitator that oil-containing solid phase and solvent are fully mixed, leaching time 30min.
After having leached, in leacher, oil-containing solid phase and solvent mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with solvent-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is solvent-oily mixed solution, enters evaporation unit.
Evaporative process utilizes steam heating, vapor temperature 125 degrees Celsius, and vapor pressure 4 kilograms, solvent vapour enters condensing equipment.
Leacher is connected with condensing equipment with dry desolventizing machine, and the solvent vapo(u)r in equipment enters condensing equipment, recycling design
Condensing equipment is circulating water cooling device, condensing temperature 20 degrees Celsius, and solvent recovering rate >96% after condensation, condensation recovered solvent loops back leacher again by pump.
Be separated in the synthesis base obtained after solvent through pervaporation, solid content 8%, maximum solid phase particle diameter is about 50um, and median particle diameter is about 10um, mud viscosity 50s, reaches the technical indicator of configuration synthesis base mud.
Oleaginousness 0.8% in final solid formation, the rate of recovery 94% of synthesis base, solvent loss 1.5%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
embodiment 6
The present embodiment is arranged in oil field, Xinjiang oil-base mud drilling engineering, adopts in the processing item of biological oil base abendoned oil base mud and oil-contained drilling cuttings, and adopting design to appraise and decide treatment scale is 2.0m
3/ h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 3.5cm, and after charging screen cloth, solid phase maximum particle diameter is 2.4cm, and median particle diameter is about 1.1mm, and solid phase liquid content is about 15%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.In centrifuging process implementing process comprehensive preferably 1.5,2.0,3.0, the filter screen in 4.0mm aperture carries out centrifuging.Centrifugal rotational speed is 1000r/min, and different pore size centrifuging implementation result is shown in table 16.
Table 16
Consider treatment capacity and reclaim quality of mud fluid, during centrifuging aperture of filter screen 3.0mm, treatment effect is best, and in implementation process, under the 3mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are shown in table 17.
Table 17
What preferred filtration efficiency was higher is 3.0mm aperture filter screen, and centrifugal rotational speed is 1000r/min, and in centrifuging, residence time of material is 6s.Roughing out slurry transportation enters in surge tank, and mix with the qualified mud of backflow, after homogeneous, reach and enter centrifugal settling equipment requirements, roughing out mud is 1:1 with the ratio of backflow mud, after mixing homogeneous, Gu containing being 42%, and feed mud viscosity, 266s.Under different rotating speeds condition, the treatment effect of centrifugal settling equipment is shown in table 18.
Table 18
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump, and field conduct shows that centrifugal settling equipment rotating speed is 1500r/min, and rotary drum and pushing spiral differential are 450r/min.Result of implementation shows after two-stage is separated, in oil base drilling wastes, the rate of recovery of biological oil base is about 52%, solid content 18% in biological oil base, maximum solid phase particle diameter is about 55um, median particle diameter is about 10um, and emulsion-breaking voltage ES is 962mV, mud viscosity 145s, six speed (3,6,100,200,300,600r/min) measurement result be: 22/58/114/138/196/274, reclaim mud and reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 9%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by leaching technology, in the present embodiment, solvent adds with the ratio of 1:1 according to mass ratio, leacher is put at solvent leacher top, leaching oil base mud or drilling cuttings, leacher adopts agitator that oil-containing solid phase and solvent are fully mixed, leaching time 15min.
After having leached, in leacher, oil-containing solid phase and solvent mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with solvent-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is solvent-oily mixed solution, enters evaporation unit.
Evaporative process utilizes steam heating, vapor temperature 120 degrees Celsius, vapor pressure 1.6 kilograms.Solvent vapour enters condensing equipment.
Leacher is connected with condensing equipment with dry desolventizing machine, and the solvent vapo(u)r in equipment enters condensing equipment, recycling design
Condensing equipment is circulating water cooling device, condensing temperature 20 degrees Celsius, and solvent recovering rate >96% after condensation, condensation recovered solvent loops back leacher again by pump.
Be separated in the biological oil base obtained after solvent through pervaporation, solid content 8%, maximum solid phase particle diameter is about 50um, and median particle diameter is about 10um, mud viscosity 50s, reaches the technical indicator configuring biological oil-base mud.
Oleaginousness 0.8% in final solid formation, the rate of recovery 94% of biological oil base, solvent loss 1.5%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
embodiment 7
The present embodiment is arranged in oil field, Xinjiang oil-base mud drilling engineering, adopts mineral oil based to discard in the processing item of oil-base mud and oil-contained drilling cuttings, and adopting design to appraise and decide treatment scale is 2.2m
3/ h, investigates the treatment capacity of technique, treatment effect and technology stability.
First raw material carries out pre-separation by charging screen cloth, and mesh size is 3.0cm, and after charging screen cloth, solid phase maximum particle diameter is 2.0cm, and median particle diameter is about 0.7mm, and solid phase liquid content is about 16%.
Raw material after pre-separation enters centrifugal separation system, and centrifugal separation processes is the coupling of centrifuging and centrifugal settling process.In centrifuging process implementing process comprehensive preferably 1.5,2.0,3.0, the filter screen in 4.0mm aperture carries out centrifuging.Centrifugal rotational speed is 1000r/min, and different pore size centrifuging implementation result is shown in table 19.
Table 19
Consider treatment capacity and reclaim quality of mud fluid, during centrifuging aperture of filter screen 2.0mm, treatment effect is best, and in implementation process, under the 2mm filter screen condition optimized, treatment effect and the system stability of different rotating speeds system are shown in table 20.
Table 20
What preferred filtration efficiency was higher is 2.0mm aperture filter screen, and centrifugal rotational speed is 1000r/min, and in centrifuging, residence time of material is 6s.Roughing out slurry transportation enters in surge tank, and mix with the qualified mud of backflow, after homogeneous, reach and enter centrifugal settling equipment requirements, roughing out mud is 1:1 with the ratio of backflow mud, after mixing homogeneous, Gu containing being 34%, and feed mud viscosity, 213s.Under different rotating speeds condition, the treatment effect of centrifugal settling equipment is shown in table 21.
Table 21
Mud in surge tank after homogeneous pumps into centrifugal settling equipment by slush pump, and field conduct shows that centrifugal settling equipment rotating speed is 1500r/min, and rotary drum and pushing spiral differential are 450r/min.Result of implementation shows after two-stage is separated, in oil base drilling wastes, the rate of recovery of mineral oil based is about 56%, solid content 21% in mineral oil based, maximum solid phase particle diameter is about 50um, median particle diameter is about 12um, and emulsion-breaking voltage ES is 916mV, mud viscosity 134s, six speed (3,6,100,200,300,600r/min) measurement result be: 26/64/98/145/188/284, reclaim mud and reach reuse standard, in solid formation, pollutant load reduces greatly, petroleum content 9%.
Low oil-containing solid phase realizes the removal of oil content in solid phase by leaching technology, in the present embodiment, solvent adds with the ratio of 1:1 according to mass ratio, leacher is put at solvent leacher top, leaching oil base mud or drilling cuttings, leacher adopts agitator that oil-containing solid phase and solvent are fully mixed, leaching time 30min.
After having leached, in leacher, oil-containing solid phase and solvent mixture are through screen filtration, and the macrobead solid of particle diameter >2mm is transported to moisture eliminator by airtight chain scraper machine; The solid particulate of particle diameter <2mm is transported to horizontal screw centrifuge by spiral pump together with solvent-oily mixed solution.Liquid holdup <20% in solid phase after horizontal screw centrifuge is separated, is transported to moisture eliminator by airtight chain scraper machine; Solid content <15% in the liquid phase be separated, is solvent-oily mixed solution, enters evaporation unit.
Evaporative process utilizes steam heating, vapor temperature 116 degrees Celsius, vapor pressure 1.4 kilograms.Solvent vapour enters condensing equipment.
Leacher is connected with condensing equipment with dry desolventizing machine, and the solvent vapo(u)r in equipment enters condensing equipment, recycling design
Condensing equipment is circulating water cooling device, condensing temperature 40 degrees Celsius, and solvent recovering rate >95% after condensation, condensation recovered solvent loops back leacher again by pump.
Be separated in the mineral oil based obtained after solvent through pervaporation, solid content 8%, maximum solid phase particle diameter is about 50um, and median particle diameter is about 10um, mud viscosity 50s, reaches the technical indicator of configuration mineral oil based muds.
Oleaginousness 0.8% in final solid formation, the rate of recovery 94% of mineral oil based, solvent loss 1.5%, and treating processes is carried out all at normal temperatures and pressures, treatment time is short, and facility investment and running cost are all lower, has significant environmental benefit, Social benefit and economic benefit.
Claims (8)
1. one kind is reclaimed oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: described recovery process comprises centrifuging, centrifugal settling, medicament normal-temperature deep desorption, distillation condensation process, and the medicament reclaimed in distillation condensation process returns the process recycled in normal-temperature deep desorption process again; Homogenizing process is had between described centrifuging, centrifugal settling process; Described homogenizing process is to be carried out with the qualified mud that centrifugal settling is produced by the roughing out mud that centrifugal filter is produced mixing, reenter in centrifugal settling equipment after homogeneous and carry out centrifugal settling and be separated.
2. one according to claim 1 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: described recovery process also comprises fed filtration process, fed filtration screen distance 2-3cm.
3. one according to claim 1 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: in described centrifugal filtration process, spin-on filter device rotating speed is 400-3000r/min.
4. one according to claim 3 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: spin-on filter device filtering net aperture 0.5-4.0mm in described centrifuging.
5. the one according to any one of claim 1-4 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: in described centrifugal settling process, in centrifugal settling equipment, rotary drum rotating speed is 600-3000r/min, rotary drum and pushing spiral differential are <300r/min.
6. one according to claim 5 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: described medicament normal-temperature deep desorption is added than the ratio with 0.7/1 ~ 1/1 according to quality of mud fluid by medicament, medicament reactor head puts into reactor, degree of depth desorption time 10 ~ 30min.
7. one according to claim 1 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: in described distillation condensation process, evaporative process utilizes steam heating, vapor temperature 110 ~ 125 DEG C, vapor pressure 1 ~ 4 kilogram.
8. one according to claim 1 reclaims oil-base mud and oil base technique from oil-base mud drilling wastes, it is characterized in that: in described distillation condensation process, condensing temperature 20 ~ 40 degrees Celsius, medicament rate of recovery >95% after condensation.
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| CN115263209B (en) * | 2022-07-29 | 2024-01-23 | 新疆天下投环保科技股份有限公司 | Method for recycling oil-based mud from oil-based mud drilling waste |
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