CN106118719A - A kind of method and apparatus removing mixing water in high boiling point high-viscosity oil - Google Patents
A kind of method and apparatus removing mixing water in high boiling point high-viscosity oil Download PDFInfo
- Publication number
- CN106118719A CN106118719A CN201610494576.7A CN201610494576A CN106118719A CN 106118719 A CN106118719 A CN 106118719A CN 201610494576 A CN201610494576 A CN 201610494576A CN 106118719 A CN106118719 A CN 106118719A
- Authority
- CN
- China
- Prior art keywords
- oil
- water
- dehydrating tower
- heat exchanger
- boiling point
- 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.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1033—Oil well production fluids
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention belongs to petrochemical industry, be specifically related to high boiling point high-viscosity oil is removed the method and apparatus of mixing water.High boiling point high-viscosity oil and aqueous mixtures, through one or more levels heat exchanger heat exchange, utilize boiling point difference wherein will be converted into gaseous state by aqueous water, enter miscella dehydrating tower；The negative pressure utilizing centrifugal force field to cause in dehydrating tower, makes the vaporous water being dissolved in oil assemble at centrifugal force field central negative nip, and isolated vaporous water flows out through top, after one or more levels heat exchanger heat exchange, is converted into aqueous water, sends into follow-up equipment；The isolated oil of dehydrating tower is flowed out by bottom, through transport pump to subsequent processes equipment.The inventive method process is simple, and equipment is few, and operation is simple, and economic benefits has a extensive future.Present invention also offers a kind of device removing mixing water in high boiling point high-viscosity oil.
Description
Technical field
The invention belongs to petrochemical industry, a kind of method relating to removing mixing water in oil, it is particularly well-suited to high boiling point
High-viscosity oil is removed mixing water process.Specifically, the invention provides in high boiling point high-viscosity oil
Method and apparatus except mixing water.
Background technology
Along with the prolongation of oilfield exploitation time, the pressure of ground base oil layer is gradually reduced.In order to extend the exploitation of oil well
In the life-span, improving recovery ratio, in oil field development, mode frequently with artificial recharge keeps the pressure of oil reservoir.Meanwhile,
Water in neighbouring stratum also can penetrate into oil reservoir, makes the moisture content of crude oil raise.
Oil is originally immiscible biphase with water, along with the fast development of Chemical Engineering Technology, and multiple active chemical reagent
It is used widely, and these active chemical reagent, make this immiscible profit the most easily be formed mutually
Stable emulsion.For only needing the industrial circle of oil phase or aqueous phase, stable emulsion can bring bigger negative shadow to it
Ring.Facing oil-water mixture because causing containing a large amount of activating agents and form stable emulsion and the difficult problem separated, profit divides
Arise at the historic moment from technology.Physical partition method is oil-water separation method the earliest, and application is relatively wide, and its advantage is will not to mix to profit
Closing liquid and bring new pollution and impurity, be disadvantageous in that oil-water separation is thorough not, the oil-water separation time is long, and equipment accounts for
Ground area is big.Physical partition method specifically includes that gravitational method, centrifuging, coarse separation method and some householder methods.Chemical method includes
Coagulant sedimentation and oxidizing process, oil removal rate height, high treating effect, can operate continuously, but chemical method equipment takes up an area big, and energy consumption is big,
A certain amount of chemical reagent need to be used.And bioanalysis does not only exist equipment and takes up an area big problem, whole process duration is the most long.
Since entering new century, oily water separation technique obtains in multiple fields such as petrochemical industry, sewage disposal, food engineerings
To extensively application.And due to organism kinds contained in oil mixing with water state, profit content, oil-water mixture, oil-water separation
The difference of the many factors such as object, causes oil-water separation difficulty to become increasing, and single oily water separation technique can not meet
Development of modern industry and the demand of environmental conservation, multiple oily water separation technique based on different operating principle is raw therewith, and is
Meet the demand of varying environment, purpose and treatment effect, different oily water separation techniques should be used for different objects.
For overcoming problem above, the present invention uses various ways to carry out triple dewatering, develops one and can reduce cost,
Simplified system, improves dehydrating effect and the oil water mixture water-eliminating method for the treatment of capacity and device thereof simultaneously.
Summary of the invention
A kind of method and apparatus removing mixing water in high boiling point high-viscosity oil, it is characterised in that:
(1) primary dewatering: the mixture of high boiling point high-viscosity oil and water enters one or more levels heat exchanger and adds thermal medium and carry out
Heat exchange, oil water mixture is tangentially entered liquid degassing cyclonic separation cylindrical section, the vaporous water after heating by dehydrating tower centre entrance
From cylindrical center, axle exhaustor flow to dehydrating tower top；Dehydrating tower utilizes boiling point difference to heat oil water mixture, initial gross separation；
(2) second dehydration: utilize oil water mixture cyclonic separation effect, in dehydrating tower, liquid degassing cyclonic separation cylindrical section is formed
Lasting cyclonic separation, forms the centrifugal negative pressuren zone of central shaft, utilizes gas dissolubility difference in the liquid of different pressures to make
The steam must being dissolved in oil is enriched with to cylindrical center's axle region, thus the further separation to steam, isolate liquid
Water flow to dehydrating tower top from cylindrical center's axle exhaustor；
(3) triple dewatering: utilize flash distillation to separate oil water mixture, the miscella after centrifugal negative pressure separates sprays into bottom flash distillation
Umbrella, steam is flashed further from miscella, forms triple dewatering；Oil after dehydration is taken off with miscella by flash distillation umbrella
The annular space runner formed between water tower wall sinks down into oil phase relief area, aggregated after flowed out by bottom miscella dehydrating tower；
After this method triple dewatering, de-water ratio reaches more than 99%.
Further, adding thermal medium in the method heat exchanger is high temperature circulation oil, and cooling medium is cold cycle oil.
Further, described heat exchanger is vertical or horizontal heat exchanger.
Further, miscella enters one or more levels heat exchanger through the aqueous vapor that dehydrating tower top is flowed out and enters with cooling medium
Row heat exchange, is cooled to liquid, sends into follow-up equipment and uses；Bottom miscella dehydrating tower flow out oil through transport pump to subsequent processes
Equipment.
The present invention also provides for a kind of device removing the employing of mixing water method in high boiling point high-viscosity oil, this device bag
Include:
Utilization adds thermal medium and aqueous water in oil water mixture is heated to the heating heat exchanger of gaseous state；
The dehydrating tower being connected with heating heat exchanger, inside is provided with the liquid cyclone degassing of gas phase and liquid phase in oil-water separation mixture
Cylindrical section, the flash distillation umbrella that vaporous water a small amount of in oil water mixture is separated connected with this liquid cyclone degassing cylindrical section；Flash distillation
The oil phase relief area for assembling oil phase it is provided with below umbrella；
Utilizing cooling medium that vaporous water is cooled to the cooling heat exchanger of aqueous water, this cooling heat exchanger is with dehydrating tower top even
Connect.
Further, described liquid cyclone degassing cylindrical section is serial or parallel connection.
Further, described flash distillation umbrella is positioned at dehydrating tower bottom, and the lower end diameter of flash distillation umbrella with the diameter ratio of dehydrating tower is
0.6～0.9.
The method characteristic of the present invention is as follows:
(1) the method comprises triple dewatering process, and dewatering efficiency reaches more than 99%, and dehydration is thoroughly.
(2) liquid cyclone degassing cylindrical section can series and parallel, be effectively improved oil water mixture dehydrating effect, increase treating capacity.
(3) in heat exchanger recycle oil can life-time service, heat exchanger can be vertical or horizontal, one or more levels.
(4) mixing water process is removed during the method is particularly well-suited to high boiling point high-viscosity oil.
Assembly of the invention feature is as follows:
The equipment used have easy of integration, simple to operate, floor space is little, dewatering efficiency is high, it is excellent to be easy to later period maintenance replacing etc.
Point, can be widely applied to field of petrochemical industry.
Accompanying drawing explanation
Fig. 1 is the method flow diagram removing mixing water in high boiling point high-viscosity oil.
Fig. 2 is dehydrating tower equipment schematic diagram.
Symbol description:
1 heating heat exchanger；2 dehydrating towers；3 liquid cyclone degassing cylindrical sections；
4 flash distillation umbrellas；5 cooling heat exchangers；6 pumps.
Detailed description of the invention
The technology design of the present invention is as follows:
As shown in Figure 1 and Figure 2, low-temperature oil aqueous mixtures enters in one or more levels heating heat exchanger 1, adds thermal medium with recycle oil
Carrying out heat exchange, after heat exchange, low-temperature oil aqueous mixtures temperature is increased to more than 100 DEG C, centre entrance enter in dehydrating tower 2, circulation
Oil is by exiting into recycle oil system bottom heating heat exchanger 1；Oil water mixture is entered liquid degassing by dehydrating tower 2 centre entrance
In cyclonic separation cylindrical section 3, in oil water mixture, vaporous water flow to dehydrating tower 2 top from cylindrical center's axle exhaustor, forms one
Secondary dehydration；Remaining oil aqueous mixtures produces in liquid cyclone degassing cylindrical section 3 and continues cyclonic separation, makes to be dissolved in W/O and steams
Gas flow to dehydrating tower 2 top from cylindrical center's axle exhaustor, forms second dehydration；After cyclonic separation, oil water mixture is revolved by liquid
Enter flash distillation umbrella 4 bottom stream degassing cylindrical section 3, make to be dissolved in W/O steam flash distillation to dehydrating tower 2 top, is formed three times de-
Water；Oil after dehydration is sunk down into oil phase relief area by the annular space runner formed between flash distillation umbrella 4 and dehydrating tower 2 tower wall, aggregated
After by bottom miscella dehydrating tower flow out；The water (gas) that dehydrating tower 2 top is flowed out enters one or more levels cooling heat exchanger 5 and follows
Ring oil cooling medium carries out heat exchange, is cooled to liquid, sends into follow-up equipment and uses；The oil flowed out bottom dehydrating tower 2 is through transport pump
To subsequent processes equipment, recycle oil is by exiting into recycle oil system bottom pump 6.
In a first aspect of the present invention, it is provided that a kind of method removing mixing water in high boiling point high-viscosity oil, the method
Including:
The mixture of high boiling point high-viscosity oil and water enters one or more levels heat exchanger, and (recycle oil) carries out heat exchange with adding thermal medium,
Make oil water mixture temperature be increased to more than 100 DEG C, utilize boiling point difference wherein will be converted into gaseous state by aqueous water, and boiling point is high
Being still liquid in the oil of 100 DEG C, but its viscosity declines owing to temperature raises, profit (gas) mixture after heat exchange is entered by middle part
Mouth entrance dehydrating tower；
Connecing liquid degassing cyclonic separation cylindrical section in dehydrating tower centre entrance, profit (gas) mixture is tangentially entered by centre entrance
Liquid degassing cyclonic separation cylindrical section, the vaporous water after heating flow to dehydrating tower top from cylindrical center's axle exhaustor, forms one
Secondary dehydration；Fluid oil declines due to viscosity, can form lasting cyclonic separation effect, in turn result in the centrifugal negative pressure of central shaft
District, utilizes the steam that gas dissolubility difference in the liquid of different pressures makes to be dissolved in oil to cylindrical center's axle region
Enrichment, thus carry out the second dehydration to steam, separating water outlet (gas) is also to flow to dehydrating tower from cylindrical center's axle exhaustor
Top；Miscella after centrifugal negative pressure separates sprays into bottom flash distillation umbrella, and now the pressure moment of miscella reduces, and causes flash distillation to imitate
Really, umbrella plane not only improves miscella flowing, also can accelerate the flash distillation speed of steam, and steam is the most further from mixing
Oil is flashed, forms triple dewatering；Oil after dehydration is by the annular space formed between flash distillation umbrella and miscella dehydrating tower wall
Runner sinks down into oil phase relief area, aggregated after flowed out by bottom miscella dehydrating tower；
The water (gas) that miscella dehydrating tower top is flowed out enters one or more levels heat exchanger and changes with cooling medium (recycle oil)
Heat, is cooled to liquid, sends into follow-up equipment and uses；The oil flowed out bottom miscella dehydrating tower sets to subsequent processes through transport pump
Standby.
In the present invention, miscella dehydrating tower operation pressure drop is 1～5kpa.
In the present invention, liquid degassing cyclonic separation cylindrical section carries out serial or parallel connection, can improve removal mixing water in oil
Effect, improves treating capacity.
In the present invention, ionic surfactant material is contained in oil phase relief area, can reduce the surface tension of solution, make
Oil phase is easily enriched with.
In a second aspect of the present invention, it is provided that a kind of high boiling point high-viscosity oil is removed the device of mixing water, this device
Including:
Heating heat exchanger, utilization adds thermal medium and aqueous water in oil water mixture is heated to gaseous state；
The dehydrating tower being connected with heating heat exchanger, including: liquid cyclone degassing cylindrical section, in oil-water separation (gas) mixture
Gas phase and liquid phase；The flash distillation umbrella being connected with liquid cyclone degassing cylindrical section, for by vaporous water a small amount of in profit (gas) mixture
Separate；Oil phase relief area, is used for assembling oil phase；
The cooling heat exchanger being connected with dehydrating tower, utilizes cooling medium that vaporous water is cooled to liquid；
The advantage of the inventive method and device is:
The method comprises triple dewatering process, and dewatering efficiency reaches more than 99%, and dehydration is thoroughly；Liquid cyclone
Degassing cylindrical section can series and parallel, be effectively improved oil water mixture dehydrating effect, increase treating capacity；Recycle oil in heat exchanger
Can life-time service, heat exchanger can be vertical or horizontal, one or more levels；The method is particularly well-suited in high boiling point high-viscosity oil
Except mixing water process；This equipment have easy of integration, simple to operate, floor space is little, dewatering efficiency is high, be easy to later period maintenance change
Etc. advantage, can be widely applied to field of petrochemical industry.
Above said content is only the basic explanation under present inventive concept, and according to appointing that technical scheme is made
What equivalent transformation, all should belong to protection scope of the present invention.Below in conjunction with embodiment, the present invention is further described, embodiment
It does not limit the scope of the invention.
Embodiment
The a certain newly-built 300,000 tons/year of coal tar hydrogenating project miscella dehydrating towers in Henan enter according to the inventive method and device
OK.
As shown in Figure 1 and Figure 2, prevailing operating conditions and dielectric property are as follows for concrete grammar flow process:
Operating mode one: dehydrating tower charging is the mixing oil product of carbolineum and washing oil, wherein carbolineum: washing oil=2:1.Inlet amount is 9.375t/
H, feeding temperature is 185 DEG C, pressure 0.3MPa.
Operating mode two: dehydrating tower charging is carbolineum, washing oil and the mixing oil product of stage casing oil, wherein carbolineum 6.25t/h, washing oil
3.125t/h, stage casing oil 9.375t/h, feeding temperature is 185 DEG C, pressure 0.3MPa.
Technique effect:
Owing to using the inventive method and device, miscella dehydrating tower operating flexibility is 50% ~ 125%, design service life 15 years,
Cycle of operation was more than 4 years continuously.Time properly functioning, when inlet water content is not more than 10000ppm, water outlet content is not more than
100ppm.The import and export pressure drop guarantee value of miscella dehydrating tower is: when operational load is 100%, pressure drop is not more than 0.05MPa,
When load is 125%, pressure drop is not more than 0.1MPa.Comparing with additive method and device, the method and device of the present invention simplifies
System, provides cost savings, and can produce great economic benefit.
The explanation of above example is only intended to help to understand method and the core concept thereof of the present invention.It is right to it should be pointed out that,
For those skilled in the art, under the premise without departing from the principles of the invention, it is also possible to the present invention is carried out
Some improvement and modification, these improve and modify in the protection domain also falling into the claims in the present invention.To disclosed enforcement
The described above of example, makes professional and technical personnel in the field be capable of or uses the present invention.Multiple amendment to these embodiments
Will be apparent from for those skilled in the art, generic principles defined herein can be without departing from this
In the case of the spirit or scope of invention, realize in other embodiments.Therefore, the present invention is not intended to be limited to illustrated herein
These embodiments, and be to fit to the widest scope consistent with principles disclosed herein and features of novelty.
Claims (7)
1. the method removing mixing water in high boiling point high-viscosity oil, comprises the following steps:
(1) primary dewatering: the mixture of high boiling point high-viscosity oil and water enters one or more levels heat exchanger and adds thermal medium and carry out
Heat exchange, oil water mixture is tangentially entered liquid degassing cyclonic separation cylindrical section, the vaporous water after heating by dehydrating tower centre entrance
From cylindrical center, axle exhaustor flow to dehydrating tower top；Dehydrating tower utilizes boiling point difference to heat oil water mixture, initial gross separation；
(2) second dehydration: utilize oil water mixture cyclonic separation effect, in dehydrating tower, liquid degassing cyclonic separation cylindrical section is formed
Lasting cyclonic separation, forms the centrifugal negative pressuren zone of central shaft, utilizes gas dissolubility difference in the liquid of different pressures to make
The steam must being dissolved in oil is enriched with to cylindrical center's axle region, thus the further separation to steam, isolate liquid
Water flow to dehydrating tower top from cylindrical center's axle exhaustor；
(3) triple dewatering: utilize flash distillation to separate oil water mixture, the miscella after centrifugal negative pressure separates sprays into bottom flash distillation
Umbrella, steam is flashed further from miscella, forms triple dewatering；Oil after dehydration is taken off with miscella by flash distillation umbrella
The annular space runner formed between water tower wall sinks down into oil phase relief area, aggregated after flowed out by bottom miscella dehydrating tower；
After this method triple dewatering, de-water ratio reaches more than 99%.
Method the most according to claim 1, it is characterised in that adding thermal medium in the method heat exchanger is high temperature circulation oil,
Cooling medium is cold cycle oil.
Method the most according to claim 1, it is characterised in that described heat exchanger is vertical or horizontal heat exchanger.
Method the most according to claim 1, it is characterised in that the aqueous vapor that miscella flows out through dehydrating tower top enters one-level
Or multi-stage heat exchanger carries out heat exchange with cooling medium, it is cooled to liquid, sends into follow-up equipment and use；Flow bottom miscella dehydrating tower
The oil gone out through transport pump to subsequent processes equipment.
5. in high boiling point high-viscosity oil, remove the device that mixing water method uses, this device bag according to claim 1 one kind
Include:
Utilization adds thermal medium and aqueous water in oil water mixture is heated to the heating heat exchanger of gaseous state；
The dehydrating tower being connected with heating heat exchanger, inside is provided with the liquid cyclone degassing of gas phase and liquid phase in oil-water separation mixture
Cylindrical section, the flash distillation umbrella that vaporous water a small amount of in oil water mixture is separated connected with this liquid cyclone degassing cylindrical section；Flash distillation
The oil phase relief area for assembling oil phase it is provided with below umbrella；
Utilizing cooling medium that vaporous water is cooled to the cooling heat exchanger of aqueous water, this cooling heat exchanger is with dehydrating tower top even
Connect.
Device the most according to claim 5, it is characterised in that liquid cyclone degassing cylindrical section is serial or parallel connection.
Device the most according to claim 5, it is characterised in that flash distillation umbrella is positioned at dehydrating tower bottom, and the lower end of flash distillation umbrella is straight
Footpath is 0.6～0.9 with the diameter ratio of dehydrating tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610494576.7A CN106118719B (en) | 2016-06-30 | 2016-06-30 | A kind of method and apparatus for being used in higher boiling high-viscosity oil remove mixing water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610494576.7A CN106118719B (en) | 2016-06-30 | 2016-06-30 | A kind of method and apparatus for being used in higher boiling high-viscosity oil remove mixing water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106118719A true CN106118719A (en) | 2016-11-16 |
| CN106118719B CN106118719B (en) | 2018-01-19 |
Family
ID=57284294
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610494576.7A Active CN106118719B (en) | 2016-06-30 | 2016-06-30 | A kind of method and apparatus for being used in higher boiling high-viscosity oil remove mixing water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106118719B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112892001A (en) * | 2021-01-13 | 2021-06-04 | 青岛理工大学 | Microbubble axial flow and rotational flow double-field three-stage pipe type T-shaped degassing device |
| CN113476881A (en) * | 2021-07-31 | 2021-10-08 | 陈翠娥 | Rosin resin ink production waste gas treatment equipment and operation method thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101397506A (en) * | 2008-08-28 | 2009-04-01 | 上海华畅环保设备发展有限公司 | Diesel oil dewatering process and apparatus |
| WO2015184464A1 (en) * | 2014-05-30 | 2015-12-03 | Fluor Technologies Corporation | Configurations and methods of dewatering crude oil |
-
2016
- 2016-06-30 CN CN201610494576.7A patent/CN106118719B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101397506A (en) * | 2008-08-28 | 2009-04-01 | 上海华畅环保设备发展有限公司 | Diesel oil dewatering process and apparatus |
| WO2015184464A1 (en) * | 2014-05-30 | 2015-12-03 | Fluor Technologies Corporation | Configurations and methods of dewatering crude oil |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112892001A (en) * | 2021-01-13 | 2021-06-04 | 青岛理工大学 | Microbubble axial flow and rotational flow double-field three-stage pipe type T-shaped degassing device |
| CN113476881A (en) * | 2021-07-31 | 2021-10-08 | 陈翠娥 | Rosin resin ink production waste gas treatment equipment and operation method thereof |
| CN113476881B (en) * | 2021-07-31 | 2023-03-31 | 陈翠娥 | Rosin resin ink production waste gas treatment equipment and operation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN106118719B (en) | 2018-01-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101070507B (en) | Regeneration method for waste lubricant and apparatus | |
| CN201008761Y (en) | Gas-liquid-solid mixed phase flow separating device for stone oil project | |
| CN105324462A (en) | Improved separation of solid asphaltenes from heavy liquid hydrocarbons using novel apparatus and process ('IAS') | |
| CN104788003B (en) | A kind of oily sludge vacuum drying method | |
| WO2014117633A1 (en) | Method and apparatus for improving hydrogen utilization rate of hydrogenation apparatus | |
| CN106118719A (en) | A kind of method and apparatus removing mixing water in high boiling point high-viscosity oil | |
| CN106730962A (en) | Condensing source heat pump Subcooled heat recovery drives single-effect distillator | |
| CN103320161A (en) | Method and apparatus for improving hydrogen utilization rate of hydrogenation equipment | |
| CN105110396B (en) | Method and device for continuously separating low-boiling point substances in wastewater produced by extraction of natural gas and shale gas | |
| CN107245348A (en) | The electric dehydration handling process and device of crude oil Produced Liquid containing complicated emulsion | |
| CN203360386U (en) | Device for improving hydrogen utilization rate of hydrogenation equipment | |
| CN206276054U (en) | Condensing source heat pump backheat drives multiple-effect distillation device | |
| CN103470951A (en) | Exhaust gas recycling device for gathering tank | |
| CN105779028B (en) | Raw coke oven gas heat and change based on washing rectifying produce the method recycled simultaneously | |
| CN203694638U (en) | Energy-saving flow system for deepwater gas field development | |
| CN103145306A (en) | Combined process and device for processing oily sludge through supercritical extraction method | |
| CN207187144U (en) | Condensing source heat pump Subcooled heat recovery driving single-effect distillator | |
| CN105062575A (en) | Process and apparatus for controlling continuous and stable discharge of non-condensable gas in benzene recovery system | |
| CN206995904U (en) | Condensing source heat pump driving multiple-effect horizontal tube falling film destilling tower | |
| CN107189810A (en) | A kind of novel combination type three phases separator based on solar energy utilization technique | |
| CN206359270U (en) | Condensing source heat pump backheat independently drives multistage flash distillation device | |
| CN204417424U (en) | Super-viscous oil SAGD cyclic preheat liquid treating system | |
| CN103668490B (en) | A kind of polyurethane fiber dry spinning medium circulation method and system | |
| CN206916078U (en) | A kind of novel combination type three phases separator based on solar energy utilization technique | |
| CN208526214U (en) | A kind of de- benzene device of low energy consumption local decompression |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |