CN103736360B - Discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings - Google Patents
Discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings Download PDFInfo
- Publication number
- CN103736360B CN103736360B CN201410033210.0A CN201410033210A CN103736360B CN 103736360 B CN103736360 B CN 103736360B CN 201410033210 A CN201410033210 A CN 201410033210A CN 103736360 B CN103736360 B CN 103736360B
- Authority
- CN
- China
- Prior art keywords
- oil
- medicament
- base
- drilling cuttings
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000003814 drug Substances 0.000 title claims abstract description 219
- 238000003795 desorption Methods 0.000 title claims abstract description 80
- 238000005553 drilling Methods 0.000 title claims abstract description 75
- 238000005520 cutting process Methods 0.000 title claims abstract description 62
- 238000011084 recovery Methods 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 claims abstract description 49
- 238000009833 condensation Methods 0.000 claims abstract description 26
- 230000005494 condensation Effects 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 26
- 238000001035 drying Methods 0.000 claims abstract description 16
- 239000007788 liquid Substances 0.000 claims description 58
- 239000000843 powder Substances 0.000 claims description 34
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 32
- 230000000903 blocking effect Effects 0.000 claims description 23
- 238000004062 sedimentation Methods 0.000 claims description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims description 16
- 238000001704 evaporation Methods 0.000 claims description 13
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000003756 stirring Methods 0.000 claims description 13
- 238000011001 backwashing Methods 0.000 claims description 11
- 238000004140 cleaning Methods 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 11
- 230000003139 buffering effect Effects 0.000 claims description 5
- 239000010865 sewage Substances 0.000 claims description 4
- 238000005516 engineering process Methods 0.000 claims description 3
- 230000009969 flowable effect Effects 0.000 claims description 3
- 238000011010 flushing procedure Methods 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 3
- 239000007790 solid phase Substances 0.000 claims description 2
- 238000004821 distillation Methods 0.000 claims 1
- 238000005373 pervaporation Methods 0.000 abstract description 13
- 238000011282 treatment Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 110
- 230000032258 transport Effects 0.000 description 27
- 238000005728 strengthening Methods 0.000 description 17
- 150000001875 compounds Chemical class 0.000 description 16
- 239000007787 solid Substances 0.000 description 15
- 238000000926 separation method Methods 0.000 description 14
- 239000000203 mixture Substances 0.000 description 12
- 238000003860 storage Methods 0.000 description 11
- 239000000463 material Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- 239000002910 solid waste Substances 0.000 description 9
- 239000002283 diesel fuel Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 239000002245 particle Substances 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 239000007924 injection Substances 0.000 description 6
- 238000002347 injection Methods 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 4
- 238000003912 environmental pollution Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000002480 mineral oil Substances 0.000 description 3
- 235000010446 mineral oil Nutrition 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000004744 fabric Substances 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 239000011268 mixed slurry Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000012239 gene modification Methods 0.000 description 1
- 230000005017 genetic modification Effects 0.000 description 1
- 235000013617 genetically modified food Nutrition 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 239000002917 insecticide Substances 0.000 description 1
- 230000007269 microbial metabolism Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
Abstract
The invention belongs in oilfield drilling engineering, oil-base mud or drilling cuttings resource reclaim field, particularly relate to the medicament normal-temperature deep desorption recovery process of oil base in a kind of discarded oil-base mud or drilling cuttings.It is characterized in that: oil-base mud or drilling cuttings are successively through mass transport, normal-temperature deep desorption, drying, and the medicament reclaimed after pervaporation, condensation recirculation uses step, and oil is separated with oil-base mud or drilling cuttings, and oil base reclaims.Medicament normal-temperature deep separating process in the present invention can either realize the harmless treatment of oil-base mud or drilling cuttings, the most of oil base in oil-base mud or drilling cuttings can be reclaimed again, the medicament used almost can reclaim completely and reuse, and processing procedure is carried out all at normal temperatures and pressures, processing time is short, except steam heating, without the need to consuming water and unclassified stores, equipment investment and running cost are all lower, have significant environmental benefit, Social benefit and economic benefit.
Description
Technical field
The invention belongs in oilfield drilling engineering, oil-base mud or drilling cuttings resource reclaim field, particularly relate to the medicament normal-temperature deep desorption recovery process of oil base in a kind of discarded oil-base mud or drilling cuttings.
Background technology
Along with the development of petroleum industry, exploration, the exploitation dynamics of deep-well and ultradeep well increase day by day, oil-base mud has excellent performance, apply more and more extensive in this type of drilling engineering, in the drilling well work of the simultaneously special formation such as water-sensitive formation, saline bed, oil-base mud is also widely used.But in the application process of oil-base mud, produce a large amount of discarded oil-base mud and oil-contained drilling cuttings, if effectively do not processed and will cause great infringement to local environment.The oil-base mud that current China commonly uses is based on diesel oil based, white oil base, biological oil base, mineral oil based, synthetic oil-base, and oil-contained drilling cuttings, the mixed slurry of well cementation, leak stopping return the link such as plasma discharge, completion clear tank generation oil-containing solid waste generation individual well and be about 250-500m
3scope, the solids oil content volume ratios such as oil-contained drilling cuttings are approximately 18 ~ 30%, if effectively do not processed, while causing environmental pollution, also will cause the huge wasting of resources.
It is hazardous waste that China's clear stipulaties oil-contained drilling cuttings and waste drilling fluids disposal produce mud, but does not formulate concrete oil-contained drilling cuttings and useless slurry discharge standard thereof.Some Domestic province oilfield treatments is with when disposing oil base oil-contained drilling cuttings and useless slurry thereof, and environmental pollution norm controlling is petroleum content <2%
Oil-base mud or disposal of cuttings recovery method are just like burning method, the bioremediation etc. utilizing the oil base in microbiological oxidation decomposition drilling cuttings.Burning method cannot realize the recovery of resource, and burning process likely causes the secondary pollution of flue gas simultaneously.When adopting microbial degradation treatment technology, due to complexity and the lower dissolubility of oil base molecular structure, easy suppression microbial metabolism, more difficultly thoroughly to be degraded by microorganism, common microbial degradation has certain limitation, and pass through the reinforcing microorganism to degrade process of genetic modification, there is again certain environmental risk.
Oil base in discarded oil-base mud as refuse process, is not realized the resource reuse of oil base by this type of technique.
Summary of the invention
For upper technical problem of dealing with problems, the invention provides the medicament normal-temperature deep desorption recovery process that cost is low, the rate of recovery is high, reduce environmental pollution, do not produce oil base in a kind of oil-base mud of second time pollution or drilling cuttings.
Solve the medicament normal-temperature deep desorption recovery process of oil base in a kind of oil-base mud in the present invention of above technical problem or drilling cuttings, it is characterized in that: oil-base mud or drilling cuttings are successively through mass transport, normal-temperature deep desorption, drying, the medicament recirculation of reclaiming after pervaporation, condensation uses step, oil is separated with oil-base mud or drilling cuttings, and oil base reclaims.
Described discarded oil-base mud or drilling cuttings comprise diesel oil based, white oil base, biological oil base, mineral oil based and synthesis base and discard the oil-containing drill waste such as oil-based drilling mud, slurry tank bed mud, the mixed slurry of well cementation and oil-contained drilling cuttings.Oil base content is 8-10%.
Described medicament normal-temperature deep desorption be by medicament according to volume ratio with 0.7/1 ~ 1/1 ratio add, medicament is put into from reactor head, in the reactor by medicament normal-temperature deep desorption, wherein reactor 2-3.
In described medicament normal-temperature deep desorption, oil-containing medicament mixed liquor is discharged from liquid outlet reactor, enters surge tank; The continuous sedimentation of the fine particle that in surge tank, mixed liquor carries, the solid particle after sedimentation is discharged from buffering pot bottom sewage draining exit.The hydraulic detention time of mixed liquor in surge tank is 7 ~ 8h.
Described liquid outlet is located at from reactor bottom 0.2-0.5m place.Oil-containing medicament is extracted out from buffering pot bottom, with pump, the supernatant liquor after quiescent settling is extracted out, make to enter solid fine particulates content in the oil-containing medicament of evaporimeter and significantly reduce, avoid the blocking of heating furnace tubulation, improve the efficiency of heating surface, improve the medicament rate of recovery.
Medicament, nitrogen associating back flushing process is also comprised in described medicament normal-temperature deep desorption, reactor bottom is squeezed into from blowback lines by part medicament pump, stir the fine powder being deposited on reactor bottom taper surface, itself and medicament is made to form flowable suspension, consider the local head loss of the viscosity of mixed liquor, the particle diameter of the solid particle of precipitation, density and fluid, determine that backwashing strength is 8 ~ 10L/m
2.s, washing time is 5 ~ 8 minutes; With pump, it is extracted out from liquid outlet again, constantly circulate.While carrying out medicament recoil, by certain pressure 1.5 ~ 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, the powder of cleaning blocking liquid outlet, make the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerate solid-liquor separation speed.
In described medicament normal-temperature deep desorption, medicament blowback lines and liquid outlet are formed closed circuit.
Reactor head can be connected with condenser, and the nitrogen passed into enters condenser, and the medicament steam of stripping is reclaimed in condensation, can by normal-temperature deep desorption process and the medicament of a small amount of gasification reclaim.
Complete the discarded oil-base mud of degree of depth desorption and contain drilling cuttings after Separation of Solid and Liquid, enter drier, in the present invention, oil-base mud or drilling cuttings are after degree of depth desorption and drying, and oil content <1.0% in drilling cuttings, can throw aside as harmless object.The medicament steam produced in dry run enters condenser, and the medicament steam produced in dry run is reclaimed in condensation.
Enter evaporimeter by the oil-containing medicament mixed liquor of the sedimentation separation of surge tank, evaporimeter utilizes Steam Heating, vapor (steam) temperature 110 ~ 125 degrees Celsius, steam pressure 0.7 ~ 0.8 kilogram, and steam heats oil-containing medicament mixed liquor to 70 ~ 80 degrees Celsius by heat exchanger.The oil obtained after medicament is separated through pervaporation, every physico-chemical property meets oil-base mud requirement, medicament steam enters No. 1 condensing plant, condensation temperature 40 ~ 45 degrees Celsius, medicament rate of recovery >90% after condensation, the medicament that condensation is reclaimed loops back reactor again by pump.
Reactor, drying device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.01 ~ 0.05Mpa, prevent medicament vapour leakage in running, reduce medicament boiling point simultaneously, reduce evaporation process energy consumption.
Medicament normal-temperature deep separating process in the present invention can either realize the harmless treatment of oil-base mud or drilling cuttings, the most of oil base in oil-base mud or drilling cuttings can be reclaimed again, the medicament used almost can reclaim completely and reuse, and processing procedure is carried out all at normal temperatures and pressures, processing time is short (completes whole medicament normal-temperature deep desorption, dry and evaporation process required time is no more than 4h), except steam heating, without the need to consuming water and unclassified stores, equipment investment and running cost are all lower, there is significant environmental benefit, Social benefit and economic benefit.
Accompanying drawing explanation
Fig. 1 is the process chart in the present invention
Fig. 2 is the process chart in the embodiment of the present invention 1
Fig. 3 is the structural representation of reactor in Fig. 2
Wherein, in Fig. 2-3: 1, No. 1 reactor; 2, No. 2 reactors; 3, surge tank; 4, mixture export; 5, evaporimeter; 6, medicament steam (vapor) outlet; 7, No. 1 condenser; 8, medicament storage tank; 9, oil base outlet; 10, oil base storage tank; 11, solid formation feed-line after medicament normal-temperature deep desorption; 12, solid formation drier; 13, air compressor; 14, compressed air inlet; 15, compressed air inlet; 16, steam boiler; 17, high-temperature steam pipeline; 18, No. 2 condensers; 19, vavuum pump; 20 refrigeration machines; 21, recirculated cooling water pipeline; 22, medicament steam pipe line; 23, compressed-air line; 24, medicament recoil pipeline; 25, medicament recoil pipeline; 26, condensation medicament pipeline; 27, oil pipeline; 28, medicament reflux pipeline; 29, medicament entrance; 30, Pressure gauge; 31, thermometer; 32, screen cloth; 33, mixture export; 34, solid material inlet; 35, medicament vapor outlet port; 36 motors; 37 paddles.
Detailed description of the invention
In a kind of useless oil-base mud in the present invention or oil-based drill cuttings oil base medicament normal-temperature deep desorption recovery process in oil-base mud or drilling cuttings successively through mass transport, medicament normal-temperature deep desorption, drying, the medicament recirculation of reclaiming after pervaporation, condensation uses step, oil is separated with oil-base mud or drilling cuttings, and oil base reclaims.
In described oil-base mud or drilling cuttings, oil base content is 8-10%, medicament normal-temperature deep desorption be by medicament according to volume ratio with 0.7/1 ~ 1/1 ratio add, medicament is put into from reactor head, in the reactor by medicament liquid phase desorption, and wherein reactor 2-3.
In described medicament normal-temperature deep desorption, oil-containing medicament mixed liquor is discharged from liquid outlet reactor, enters surge tank; The continuous sedimentation of the fine particle that in surge tank, mixed liquor carries, the solid particle after sedimentation is discharged from buffering pot bottom sewage draining exit.The time of staying of mixed liquor in surge tank is 7 ~ 8h.
Described liquid outlet is located at from reactor bottom 0.2-0.5m place.Oil-containing medicament is extracted out from buffering pot bottom, with pump, the supernatant liquor after quiescent settling is extracted out, make to enter solid fine particulates content in the oil-containing medicament of evaporimeter and significantly reduce, avoid the blocking of heating furnace tubulation, improve the efficiency of heating surface, improve the medicament rate of recovery.
Medicament, nitrogen associating back flushing process is also comprised in described medicament normal-temperature deep desorption, reactor bottom is squeezed into from blowback lines by part medicament pump, stir the fine powder being deposited on reactor bottom taper surface, itself and medicament is made to form flowable suspension, consider the local head loss of the viscosity of mixed liquor, the particle diameter of the solid particle of precipitation, density and fluid, determine that backwashing strength is 8 ~ 10L/m
2.s, washing time is 5 ~ 8 minutes; With pump, it is extracted out from liquid outlet again, constantly circulate.While carrying out medicament recoil, by certain pressure 1.5 ~ 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, the powder of cleaning blocking liquid outlet, make the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerate solid-liquor separation speed.
In described normal-temperature deep desorption, medicament blowback lines and liquid outlet are formed closed circuit.
Reactor head can be connected with condenser, and the nitrogen passed into enters condenser, and the medicament steam of stripping is reclaimed in condensation, can by desorption process and the medicament of a small amount of gasification reclaim.
Complete the discarded oil-base mud of degree of depth desorption and contain drilling cuttings after Separation of Solid and Liquid, enter drier, in the present invention, oil-base mud or drilling cuttings are after degree of depth desorption and drying, and oil content <1.0% in drilling cuttings, can throw aside as harmless object.The medicament steam produced in dry run enters condenser, and the medicament steam produced in dry run is reclaimed in condensation.
Enter evaporimeter by the oil-containing medicament mixed liquor of the sedimentation separation of surge tank, evaporimeter utilizes Steam Heating, vapor (steam) temperature 110 ~ 125 degrees Celsius, steam pressure 0.7 ~ 0.8 kilogram, and steam heats oil-containing medicament mixed liquor to 70 ~ 80 degrees Celsius by heat exchanger.The oil base obtained after medicament is separated through pervaporation, every physico-chemical property meets oil-base mud requirement, medicament steam enters No. 1 condensing plant, condensation temperature 40 ~ 45 degrees Celsius, medicament rate of recovery >90% after condensation, the medicament that condensation is reclaimed loops back reactor again by pump.
Reactor, drying device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.01 ~ 0.05Mpa, prevent medicament vapour leakage in running, reduce medicament boiling point simultaneously, reduce evaporation process energy consumption.
Concrete operations can be
Embodiment 1
Medicament normal-temperature deep desorption unit adopts two reactors No. 1 reactor and No. 2 reactors, by driven by motor paddle stirring system, to reduce the thickness of cake layer; And join screen cloth, to reduce the amounts of particles entering liquid phase.Material enters reactor through material inlet, and medicament injects from top medicament entrance and carries out degree of depth desorption.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from recoil pipeline and recoil pipeline in desorption process, compressed air is squeezed into No. 1 reactor and No. 2 reactors by compressed-air line and reactor compressed air inlet by air compressor respectively simultaneously, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improves desorption efficiency.Reactor head can be connected with No. 2 condensers by medicament steam (vapor) outlet, can by desorption process and the medicament of a small amount of gasification reclaim.Oil-containing medicament after degree of depth desorption completes enters surge tank from reactor bottom eliminating, and solid is transported in solids dryer dry by solid phase feed-line.Bottom surge tank, 0.3m place establishes liquid outlet, oil-containing medicament mixed liquor through sedimentation enters evaporimeter (5) by outlet, the medicament steam of evaporation enters No. 1 condensing plant by the vapor outlet port on top, reactor, surge tank drier is connected to No. 2 condensing plants by vavuum pump, adopts tiny structure to run in running.The insecticide liquid of condensation enters medicament storage tank by condensate liquid pipeline, and condensed medicament can loop back reactor again.Condenser adopts recirculated cooling water to cool, and recirculated cooling water is freezed by refrigeration machine, is connected with No. 1 condenser by recirculated cooling water pipeline with No. 2 condensers.Heating high-temperature steam is produced by boiler, is transported to reactor by high-temperature steam pipeline, drier and evaporimeter.
For the discarded oil-based drilling mud that oil base content is about 10%, oil-base mud transports material to reactor through pusher, and conveying capacity is 0.5m
3/ h, medicament injects from reactor head and carries out degree of depth desorption, and medicament dosage is 0.5m
3/ h.Mix and blend in the reactor, the time of staying is 20min, by medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 10L/m
2.s, washing time is 8 minutes.By 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after degree of depth desorption completes pumps into surge tank.Oil-containing medicament after degree of depth desorption completes is discharged from liquid outlet, enters surge tank, and residual solid is transported in solids dryer dry by screw input feeder.Establish sewage draining exit bottom surge tank, 0.3m place, bottom establishes liquid outlet, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 125 degrees Celsius, steam pressure 0.8 kilogram, heating oil-containing medicament mixed liquor is to 80 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 40 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.05Mpa in running, and total system is 95%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The oil base rate of recovery reaches 99%, oil base content <0.6% remaining in solid waste.
Embodiment 2
Be the oil-contained drilling cuttings of about 8% for oil base content, cross pusher and transport material to reactor, conveying capacity is 0.1m
3/ h, oil-base mud carries out medicament normal-temperature deep desorption through medicament from reactor head injection, and medicament dosage is 0.07m
3/ h, in the reactor mix and blend, the time of staying is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 8L/m
2.s, washing time is 5 minutes.By 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 110 degrees Celsius, steam pressure 0.7 kilogram, heating oil-containing medicament mixed liquor is to 70 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 45 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.01Mpa in running, and total system is the medicament rate of recovery is 90%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The oil base rate of recovery reaches 99%, oil base content <1% remaining in solid waste.
Embodiment 3
For discarded diesel oil based mud and oil-contained drilling cuttings mixture that diesel oil based content is about 9%, cross pusher and transport material to reactor, conveying capacity is 3m
3/ h, medicament injects from reactor head and carries out medicament normal-temperature deep desorption, and medicament dosage is 2.4m
3/ h, the time of staying in reactor is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 9L/m
2.s, washing time is 10 minutes.By 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 115 degrees Celsius, steam pressure 0.72 kilogram, heating oil-containing medicament mixed liquor is to 75 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 42 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.01Mpa in running, and total system is the medicament rate of recovery is 94%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The diesel oil based rate of recovery reaches 99%, oil base content <0.8% remaining in solid waste.
Embodiment 4
For discarded diesel oil based mud and oil-contained drilling cuttings mixture that diesel oil based content is about 10%, cross pusher and transport material to reactor, conveying capacity is 5m
3/ h, carry out medicament normal-temperature deep desorption through medicament from reactor head injection, medicament dosage is 5m
3/ h, the time of staying in reactor is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 10L/m
2.s, washing time is 10 minutes.By 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 125 degrees Celsius, steam pressure 0.8 kilogram, heating oil-containing medicament mixed liquor is to 75 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 40 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.01Mpa in running, and total system is the medicament rate of recovery is 96%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The diesel oil based rate of recovery reaches 99%, oil base content <0.8% remaining in solid waste.
Embodiment 5
The white oil base being about 10% for oil content discards oil-base mud and oil-contained drilling cuttings mixture, and cross pusher and transport material to reactor, conveying capacity is 2m
3/ h, carry out medicament normal-temperature deep desorption through medicament from reactor head injection, medicament dosage is 2m
3/ h, the time of staying in reactor is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 10L/m
2.s, washing time is 10 minutes.By 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 125 degrees Celsius, steam pressure 0.8 kilogram, heating oil-containing medicament mixed liquor is to 75 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 40 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.01Mpa in running, and total system is the medicament rate of recovery is 92%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The oil base rate of recovery reaches 99%, oil content <0.8% remaining in solid waste.
Embodiment 6
The synthesis base being about 10% for oil content discards oil-base mud and oil-contained drilling cuttings mixture, and cross pusher and transport material to reactor, conveying capacity is 3m
3/ h, carry out medicament normal-temperature deep desorption through medicament from reactor head injection, medicament dosage is 3m
3/ h, the time of staying in reactor is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 8L/m
2.s, washing time is 5 minutes.By 1.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 110 degrees Celsius, steam pressure 0.7 kilogram, heating oil-containing medicament mixed liquor is to 70 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 42 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.05Mpa in running, and total system is the medicament rate of recovery is 95%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The oil base rate of recovery reaches 99%, oil content <0.8% remaining in solid waste.
Embodiment 7
For biological oil base abandoned oil base mud and oil-contained drilling cuttings mixture that oil content is about 10%, cross pusher and transport material to reactor, conveying capacity is 2.5m
3/ h, carry out medicament normal-temperature deep desorption through medicament from reactor head injection, medicament dosage is 2.5m
3/ h, the time of staying in reactor is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 9L/m
2.s, washing time is 6 minutes.By 2.0Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 115 degrees Celsius, steam pressure 0.72 kilogram, heating oil-containing medicament mixed liquor is to 75 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 40 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.03Mpa in running, and total system is the medicament rate of recovery is 94%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The oil base rate of recovery reaches 99%, oil content <0.8% remaining in solid waste.
Embodiment 8
The mineral oil based being about 10% for oil content discards oil-base mud and oil-contained drilling cuttings mixture, and cross pusher and transport material to reactor, conveying capacity is 4m
3/ h, carry out medicament normal-temperature deep desorption through medicament from reactor head injection, medicament dosage is 4m
3/ h, the time of staying in reactor is 15min.By medicament circulating pump, part medicament pump is squeezed into reactor bottom from blowback lines in desorption process, stir the discarded oil-base mud and the oil-contained drilling cuttings fine powder that are deposited on reactor bottom taper surface, strengthening mass transport process, improve desorption efficiency, backwashing strength is 9L/m
2.s, washing time is 8 minutes.By 2.5Mpa nitrogen squeeze into reactor bottom taper surface by the threeway in liquid outlet, strengthening solid-liquid shows mass transport process, the powder of the liquid outlet of cleaning blocking simultaneously, makes the blocking of fine powder minimizing to liquid outlet being deposited on reactor bottom taper surface, accelerates solid-liquor separation speed.Oil-containing medicament after desorption completes pumps into surge tank.Oil-containing medicament mixed liquor time of staying in surge tank is 7h, after sedimentation, is pumped in evaporimeter by the oil-containing medicament mixed liquor through sedimentation in surge tank by compound pump.Evaporimeter adopts shell and tube single effect evaporator, adopt Steam Heating, vapor (steam) temperature 120 degrees Celsius, steam pressure 0.78 kilogram, heating oil-containing medicament mixed liquor is to 78 degrees Celsius, and the medicament steam of evaporation enters No. 1 condensing plant, condensation temperature 40 degrees Celsius, condensed compound pump enters medicament storage tank, again loops back reactor by pump.Reactor, drying device and vaporising device are connected to No. 2 condensing plants by vavuum pump, adopt tiny structure to run, vacuum 0.04Mpa in running, and total system is the medicament rate of recovery is 95%.Be separated through pervaporation the oil base obtained after medicament, every physico-chemical property meets oil-base mud requirement, can again for preparing oil-base mud for drilling engineering.The oil base rate of recovery reaches 99%, oil content <0.8% remaining in solid waste.
Claims (7)
1. discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings, comprise medicament, pusher, reactor, drier and evaporative condenser, it is characterized in that: oil-base mud or drilling cuttings are successively through mass transport, medicament normal-temperature deep desorption, drying and evaporative condenser step, and the medicament reclaimed after distillation condensation recycles step, oil is separated with oil-base mud or drilling cuttings, and oil base reclaims; Described medicament normal-temperature deep desorption, puts into reactor by medicament by medicament reactor head, and oil-containing medicament is discharged from the liquid outlet reactor, enters surge tank, and the fine powder after sedimentation is discharged from buffering pot bottom sewage draining exit;
Medicament and nitrogen associating back flushing process is also comprised in described medicament normal-temperature deep desorption, the part medicament pump being about to reclaim squeezes into reactor bottom from blowback lines, stir the fine powder being deposited on reactor bottom taper surface, make itself and medicament form flowable suspension, backwashing strength is 8 ~ 10L/m
2.s, washing time is 5 ~ 8 minutes; With pump, it is extracted out from liquid outlet again, constantly circulate.
2. the medicament normal-temperature deep desorption recovery process of oil base in discarded oil-base mud according to claim 1 or drilling cuttings, it is characterized in that: described medicament normal-temperature deep desorption Chinese medicine and solid phase according to volume ratio with 0.7/1 ~ 1/1 ratio add, wherein reactor 2-3.
3., according to the medicament normal-temperature deep desorption recovery process of oil base in the discarded oil-base mud described in claim 1 or drilling cuttings, it is characterized in that: the liquid outlet on reactor is located at from 0.2-0.5m place, bottom.
4. the medicament normal-temperature deep desorption recovery process of oil base in discarded oil-base mud according to claim 1 or drilling cuttings, it is characterized in that: also comprise in medicament normal-temperature deep desorption and the nitrogen of certain pressure 1.5 ~ 2.5Mpa is squeezed into reactor bottom taper surface by the threeway in liquid outlet, the powder of cleaning blocking liquid outlet.
5. the medicament normal-temperature deep desorption recovery process of oil base in discarded oil-base mud according to claim 1 or drilling cuttings, is characterized in that: in oil-base mud or drilling cuttings, oil base content is 8-20%.
6. the medicament normal-temperature deep desorption recovery process of oil base in discarded oil-base mud according to claim 1 or drilling cuttings, it is characterized in that: evaporation technology utilizes Steam Heating, vapor (steam) temperature 110 ~ 125 DEG C, steam pressure 0.7 ~ 0.8 kilogram, steam heats oil-containing medicament mixed liquor to 70 ~ 80 DEG C by heat exchanger.
7. the medicament normal-temperature deep desorption recovery process of oil base in discarded oil-base mud according to claim 1 or drilling cuttings, is characterized in that: in described condensing steps, condensation temperature 40 ~ 45 degrees Celsius, medicament rate of recovery >90% after condensation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410033210.0A CN103736360B (en) | 2013-12-05 | 2014-01-24 | Discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310644200.6 | 2013-12-05 | ||
| CN201310644200 | 2013-12-05 | ||
| CN201410033210.0A CN103736360B (en) | 2013-12-05 | 2014-01-24 | Discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103736360A CN103736360A (en) | 2014-04-23 |
| CN103736360B true CN103736360B (en) | 2016-01-27 |
Family
ID=50493467
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410033210.0A Active CN103736360B (en) | 2013-12-05 | 2014-01-24 | Discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103736360B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104673348A (en) * | 2015-02-05 | 2015-06-03 | 重庆大学 | Method for recovering base oil from oil-based drilling mud and equipment for implementing method |
| CN108793674B (en) * | 2018-08-31 | 2023-12-12 | 河北华运鸿业化工有限公司 | Waste oil-based mud separating and recycling device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101172738A (en) * | 2007-11-13 | 2008-05-07 | 天津莱特化工有限公司 | Innocent treatment method for oil-containing sewage sludge |
| CN101269380A (en) * | 2008-05-15 | 2008-09-24 | 天津开发区兰顿油田服务有限公司 | Method for removing oil-containing drill cuttings and oil component in oil polluted soil |
-
2014
- 2014-01-24 CN CN201410033210.0A patent/CN103736360B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101172738A (en) * | 2007-11-13 | 2008-05-07 | 天津莱特化工有限公司 | Innocent treatment method for oil-containing sewage sludge |
| CN101269380A (en) * | 2008-05-15 | 2008-09-24 | 天津开发区兰顿油田服务有限公司 | Method for removing oil-containing drill cuttings and oil component in oil polluted soil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103736360A (en) | 2014-04-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110240369B (en) | Pyrolysis-extraction circulating recycling treatment process method for polymer-containing oil sludge | |
| CN103127736A (en) | Evaporation and concentration device utilizing heat pump technique | |
| CN105036507B (en) | Pyrolysis oil-gas-water synchronous condensing and oil-water separation recovery system and method | |
| CN104922974B (en) | A kind of concentration device for material liquid | |
| CN106348368A (en) | Heat pump evaporation system and heat pump evaporation method used for processing low-activity liquid waste in nuclear plant | |
| CN101787907A (en) | Steam condensate water recycling and working system and method thereof | |
| CN103736360B (en) | Discard the medicament normal-temperature deep desorption recovery process of oil base in oil-base mud or drilling cuttings | |
| CN104478135A (en) | Treatment method of salt-containing wastewater | |
| CN112066686A (en) | Novel condensation heat recovery disc type sludge low-temperature drying system | |
| CN204841160U (en) | Feed liquid enrichment facility | |
| CN101759272B (en) | Supercritical water oxidized organic wastewater treating system | |
| CN113735209A (en) | Full-quantification landfill leachate treatment device and process | |
| CN106630338B (en) | Method and device for treating organic wastewater | |
| CN102115289A (en) | Device for separating pollutant in garbage leachate | |
| CN204026651U (en) | A kind of closed condensate water recovery device | |
| CN204151096U (en) | A kind of industry contains pre-treatment and the heat reclamation device of ammonia sewage | |
| CN102115290B (en) | Method for separating pollutants from landfill leachate | |
| CN204111503U (en) | A kind of unconventional oilfield sewage treatment device | |
| CN204002656U (en) | In small-sized discarded oil-base mud and oil-contained drilling cuttings, base oil is with boring reclaimer | |
| CN206616071U (en) | Oily-water seperating equipment | |
| CN215905885U (en) | Full-quantification landfill leachate treatment device | |
| CN106630336B (en) | Method and device for treating wastewater containing organic matters | |
| CN212713185U (en) | Oil-based detritus processing apparatus | |
| CN204644309U (en) | The device that steam negative pressure benzene removal method uses | |
| CN104098151B (en) | A kind of oil gas field waste water treatment device and treatment process thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20160321 Address after: Jinjiang District Jinhua Road Chengdu City, Sichuan province 610000 section of No. 8 Building 1 11 unit 27 floor No. 2742 Patentee after: Sichuan Bo Sheng Wing Yip Engineering Technology Co Ltd Address before: Xindu Avenue in Xindu District of Chengdu city of Sichuan Province, Southwest Petroleum University No. 8 610500 Patentee before: Wang Bing Patentee before: Ren Hongyang Patentee before: Li Yuedong Patentee before: Xu Yang |
|
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20140423 Assignee: Bazhou Xin Rui Environmental Protection Technology Co., Ltd. Assignor: Sichuan Bo Sheng Wing Yip Engineering Technology Co Ltd Contract record no.: 2018510000048 Denomination of invention: Oil-based normal-temperature deep agent desorption and recovery process in waste oil-base mud or drilling cuttings Granted publication date: 20160127 License type: Common License Record date: 20180918 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| CP02 | Change in the address of a patent holder | ||
| CP02 | Change in the address of a patent holder |
Address after: 610000 510, floor 5, unit 1, building 5, No. 8, Liuli Road, Jinjiang District, Chengdu City, Sichuan Province Patentee after: Sichuan Bo Sheng Wing Yip Engineering Technology Co.,Ltd. Address before: Jinjiang District Jinhua Road Chengdu City, Sichuan province 610000 section of No. 8 Building 1 11 unit 27 floor No. 2742 Patentee before: Sichuan Bo Sheng Wing Yip Engineering Technology Co.,Ltd. |
|
| CP02 | Change in the address of a patent holder | ||
| CP02 | Change in the address of a patent holder |
Address after: 610021 No. 510, floor 5, unit 1, building 5, No. 8, Liuli Road, Jinjiang District, Chengdu City, Sichuan Province Patentee after: Sichuan Bo Sheng Wing Yip Engineering Technology Co.,Ltd. Address before: 610000 510, floor 5, unit 1, building 5, No. 8, Liuli Road, Jinjiang District, Chengdu City, Sichuan Province Patentee before: Sichuan Bo Sheng Wing Yip Engineering Technology Co.,Ltd. |
|
| EC01 | Cancellation of recordation of patent licensing contract | ||
| EC01 | Cancellation of recordation of patent licensing contract |
Assignee: Bazhou Xin Rui Environmental Protection Technology Co.,Ltd. Assignor: Sichuan Bo Sheng Wing Yip Engineering Technology Co.,Ltd. Contract record no.: 2018510000048 Date of cancellation: 20210203 |
|
| EE01 | Entry into force of recordation of patent licensing contract | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20140423 Assignee: Bazhou Xin Rui Environmental Protection Technology Co.,Ltd. Assignor: Sichuan Bo Sheng Wing Yip Engineering Technology Co.,Ltd. Contract record no.: X2021980001268 Denomination of invention: Deep desorption and recovery process of oil-based chemicals from waste oil-based mud or drilling cuttings at room temperature Granted publication date: 20160127 License type: Exclusive License Record date: 20210224 |