CN107355682B - Heavy crude petroleum originates from certainly mixes diluent device - Google Patents
Heavy crude petroleum originates from certainly mixes diluent device Download PDFInfo
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- CN107355682B CN107355682B CN201710344551.3A CN201710344551A CN107355682B CN 107355682 B CN107355682 B CN 107355682B CN 201710344551 A CN201710344551 A CN 201710344551A CN 107355682 B CN107355682 B CN 107355682B
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- connect
- tank
- flash column
- heat exchanger
- viscous crude
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
- F17D1/16—Facilitating the conveyance of liquids or effecting the conveyance of viscous products by modification of their viscosity
- F17D1/17—Facilitating the conveyance of liquids or effecting the conveyance of viscous products by modification of their viscosity by mixing with another liquid, i.e. diluting
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Public Health (AREA)
- Water Supply & Treatment (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention provides a kind of heavy crude petroleum and mixes diluent device from originating from, closed loop reducing thick oil viscosity system is formed inside viscous crude field, by the way that the process flow of viscous crude visbreaking is arranged in multi-purpose station, while by either shallow thermal cracking, a certain proportion of light component is obtained as reducing thick oil viscosity diluent；According to demand, portion of diluent is returned and is mixed to heavy crude well shaft bottom, meets the defeated demand of heavy crude well collection, another part diluent is mixed to visbreaking after-purification viscous crude, and defeated requirement outside viscous crude is met；Advantage are as follows: by either shallow thermal cracking, viscous crude viscosity reducing rate reaches 95% or more, and is suitably incorporated self-produced extra diluent, meets defeated condition outside viscous crude；The reducing thick oil viscosity diluent that production is continuously recycled by system meets the defeated demand of collection of the viscous crude from well head to multi-purpose station, thoroughly solves the problems such as mixing light oil source is insufficient, gathering system heating energy consumption is high, realizes the defeated inexpensive target of the acquisition of viscous crude.
Description
Technical field
The present invention relates to viscous crude process units fields, originate from certainly more particularly, to a kind of heavy crude petroleum and mix diluent device.
Background technique
With fast-developing and to oil demand the continuous growth of world economy, conventional oil reserves are increasingly reduced；Meanwhile
Petroleum technology progress brings heavy oil production to be continuously improved, and thickened oil recovery cost constantly reduces, and viscous crude resource will become important
Strategy takes over one of energy.
However, the heavy constituents such as the resin and asphalt content in viscous crude composition is high, light component content is few, causes the viscous of viscous crude
Spend high, relatively denser, poor fluidity.Since the viscosity of viscous crude is very high, the defeated mode of conventional tube is technically and in economy
All there are many problems, this makes viscous crude, and all there is very big difficulty in terms of developing, collecting.Heavy oil transportation and processing are most
Big to hinder to be viscosity height, how to reduce viscosity is the key that realize the production of super-viscous oil oil field high-efficiency and economic.Currently used viscous crude
Viscosity reduction conveys technique mainly include the following types: 1, single tube heating, viscosity reducing conveys；2, adding active water viscosity reduction conveys；3, thin oil blending visbreaking
Conveying；4, injection friction reducer viscosity reduction conveying etc..And the above reducing thick oil viscosity conveying technique has the limitation of different aspect.Single tube adds
More intermediate heating stations need to be arranged in the case where heavy oil transportation distance, flow are small to guarantee that viscous crude pipe is defeated in the viscous conveying of heat drop
Temperature is also unfavorable for daily production management while investment is high, energy consumption is high；Adding active water viscosity reduction technique during transportation oil,
Water is easily layered, and the viscous crude that bulk easily occurs in the viscous crude big for viscosity, condensation point is high, which suspends, to be flowed, thus blocking pipeline and equipment,
And be easy to cause pipeline corrosion, structure and multi-purpose station dehydration load increase, energy consumption increase the problems such as；Blending diluting oil technology needs to protect
Card has sufficient thin oil oil sources, and the in addition blending of viscous crude and thin oil has an impact to respective oil property, it is difficult to efficiently use thick
Oil and thin oil resource；That there are friction reducers is at high cost for injection friction reducer viscosity reduction technique, influences Water Cut Oil ' after injection friction reducer
State causes the dehydration of multi-purpose station crude oil and sewage treatment difficulty to increase.
Summary of the invention
It is an object of the invention to solve the deficiencies in the prior art, and heavy crude petroleum is provided and mixes diluent dress from originating from
It sets.
The new technical solution of the present invention is: heavy crude petroleum mixes diluent device from originating from, including return mix pump, heat exchanger, into
Expect pump, surge tank, flash column, pump, air cooler, reflux pump, heating furnace, reaction tower, fractionating column, return tank, between each device by
Pipeline connects, surge tank, flash column, reaction tower, fractionating column, return tank top installation pressure gauge and thermometer, between device
Check valve, device and pipeline are installed on pipeline by flanged joint, thick oil pipeline is directly connected to thin oil surge tank entrance, and thin oil is slow
It rushes tank side and is provided with feed opening, mix diluent material stock tank with oil well time and connect, the outlet of thin oil surge tank is connect with thin oil heat exchanger；
The thin oil outlet of thin oil heat exchanger is returned by thin oil mixes pump and transports to heavy oil wells bottom, the viscous crude outlet of thin oil heat exchanger be not dehydrated it is thick
Oil heat exchanger connection；The well liquid outlet for not being dehydrated thick oil heat exchanger connects through flash column feed pump and flash column feed exchanger
It connects, flash column feed exchanger is connect with flash column；The viscous crude outlet of flash column is through flash distillation column bottoms pump and flash column bottom heat exchanger
It is connect with heating furnace；The top exit of flash column connects flash column head space cooler, and flash column head space cooler and flash column take one's place heat
Device connection；Flash column top heat exchanger is connect with flash distillation tower buffer tank, and flash distillation tower buffer tank top exit is connect with heating furnace；
Heating furnace is connect with reaction tower, and the viscous crude outlet of reaction tower is connect with fractionating column；Fractionator overhead is connect with air cooler, and is passed through
Pipeline connects heating furnace, and tower bottom is viscous crude outlet.
The viscous crude entrance of surge tank is set to the upper lateral part of tank body, and feed opening is set to tank body side, and outlet is set to tank base；
The entrance of thin oil heat exchanger is set to tank base, and thin oil outlet is set to top of the tank, and viscous crude outlet is set to tank base, and gas enters
Mouth sets out tank body side；The top for not being dehydrated thick oil heat exchanger is equipped with viscous crude entrance, and tank body side is exported equipped with well liquid, bottom
Equipped with sewage draining exit.
The top gas outlet of the flash column feed exchanger is connect with thin oil heat exchanger.
The flash column feed exchanger heat transferring medium is communicated with flash column bottom heat exchanger heat transferring medium.
The flash distillation tower buffer tank top gas outlet is connect with heating furnace.
The air cooler is connect with fractionation return tank of top of the tower, and the outlet of fractionation return tank of top of the tower top gas connects with heating furnace
It connects.
The beneficial effects of the present invention are: viscous crude viscosity reducing rate reaches 95% or more by either shallow thermal cracking, and it is suitably incorporated certainly
Extra diluent is produced, defeated condition outside viscous crude is met；The reducing thick oil viscosity diluent that production is continuously recycled by system, meet viscous crude from
The defeated demand of the collection of well head to multi-purpose station thoroughly solves the problems such as mixing light oil source is insufficient, gathering system heating energy consumption is high, realizes viscous crude
The defeated inexpensive target of acquisition.
Detailed description of the invention
Fig. 1 is device connection diagram of the invention.
Fig. 2 is device connection diagram of the invention.
Wherein: 1 mixes pump for thin oil time, and 2 be thin oil heat exchanger, and 3 is are not dehydrated thick oil heat exchanger, and 4 be flash column feed pump,
5 be flash column feed exchanger, and 6 be thin oil surge tank, and 7 be flash column, and 8 be flash distillation column bottoms pump, and 9 be flash column head space cooler,
10 be flash column top heat exchanger, and 11 be flash distillation tower buffer tank, and 12 be flash distillation tower top return pump, and 13 be flash column bottom heat exchanger,
14 be heating furnace, and 15 be reaction tower, and 16 be fractionating column, and 17 be air cooler, and 18 be fractionation return tank of top of the tower.
Specific embodiment
The present invention will be further described with reference to the accompanying drawing.
Heavy crude petroleum mixes diluent device from originating from, including return mix pump, heat exchanger, feed pump, surge tank, flash column 7,
Pump, air cooler 17, flash distillation tower top return pump 12, heating furnace 14, reaction tower 15, fractionating column 16, return tank, by pipe between each device
Line connects, surge tank, flash column 7, reaction tower 15, fractionating column 16, return tank top installation pressure gauge and thermometer, between device
Pipeline on be installed on check valve, device and pipeline by flanged joint, thick oil pipeline is directly connected to 6 entrance of thin oil surge tank, dilute
Oily 6 side of surge tank is provided with feed opening, mixes diluent material stock tank with oil well time and connect, and the outlet of thin oil surge tank 6 exchanges heat with thin oil
Device 2 connects；The thin oil outlet of thin oil heat exchanger 2 mixes pump 1 by thin oil time and transports to heavy oil wells bottom, and the viscous crude of thin oil heat exchanger 2 goes out
Mouthful be not dehydrated thick oil heat exchanger 3 and connect；It is not dehydrated the well liquid outlet of thick oil heat exchanger 3 through flash column feed pump 4 and flash distillation
Tower feed exchanger 5 connects, and flash column feed exchanger 5 is connect with flash column 7；The viscous crude of flash column 7 is exported through flash column bottom
Pump 8 and flash column bottom heat exchanger 13 are connect with heating furnace 14；The top exit of flash column 7 connects flash column head space cooler 9, flash distillation
Tower top air cooler 9 is connect with flash column top heat exchanger 10；Flash column top heat exchanger 10 is connect with flash distillation tower buffer tank 11, is flashed
11 top exit of tower buffer tank is connect with heating furnace 14；Heating furnace 14 is connect with reaction tower 15, the viscous crude outlet of reaction tower 15
It is connect with fractionating column 16；16 tower top of fractionating column is connect with air cooler 17, and connects heating furnace 14 by pipeline, and tower bottom goes out for viscous crude
Mouthful.
The viscous crude entrance of surge tank is set to the upper lateral part of tank body, and feed opening is set to tank body side, and outlet is set to tank base；
The entrance of thin oil heat exchanger 2 is set to tank base, and thin oil outlet is set to top of the tank, and viscous crude outlet is set to tank base, gas
Entrance sets out tank body side；The top for not being dehydrated thick oil heat exchanger 3 is equipped with viscous crude entrance, and tank body side is exported equipped with well liquid,
Bottom is equipped with sewage draining exit.
The top gas outlet of the flash column feed exchanger 5 is connect with thin oil heat exchanger 2.
5 heat transferring medium of flash column feed exchanger is communicated with 13 heat transferring medium of flash column bottom heat exchanger.
11 top gas of the flash distillation tower buffer tank outlet is connect with heating furnace 14.
The air cooler 17 is connect with fractionation return tank of top of the tower 18, and fractionation 18 top gas of return tank of top of the tower exports and adds
Hot stove 14 connects.
According to the defeated demand of heavy crude well collection, a certain amount of oil well is inputted in thin oil surge tank 6 and is returned and mixes diluent, by thin oil
After heat exchanger 2 heats up, is returned by thin oil and mix pump 1 and transport to heavy oil wells bottom and carry out back mixing viscosity reduction, meet heavy oil gathering system initial state
Lower production run；Oil well after mixing diluent carrys out liquid and enters in multi-purpose station not being dehydrated after thick oil heat exchanger 3 heats up, de- through multi-purpose station
Water system dehydration, purification viscous crude is after flash column feed pump 4, flash column feed exchanger 5 heat, into flash column 7, abjection portion
Divide fixed gas and light oil.Viscous crude enters after flash distillation column bottoms pump 8 and flash column bottom heat exchanger 13 heat after the processing of flash column 7
Heating furnace 14 heats up again, until entering reaction tower 15 after specific temperature carries out light cracking visbreaking reaction.By reaction tower 15
Viscous crude afterwards enters fractionating column 16 and is fractionated, and overhead components form fixed gas and self-produced diluent after air cooler 17 is cooling,
Tower bottom is viscous crude after visbreaking.Fixed gas is used for the defeated drop of heavy crude well collection as 14 fuel combustion of system heating furnace, self-produced diluent
Defeated viscosity reduction outside viscous crude after viscous and visbreaking.
Claims (1)
1. heavy crude petroleum originates from certainly mixes diluent device, including returns and mix pump, heat exchanger, feed pump, surge tank, flash column, pump, sky
Cooler, reflux pump, heating furnace, reaction tower, fractionating column, return tank are connected by pipeline between each device, surge tank, flash column, anti-
Answer tower, fractionating column, installation pressure gauge and thermometer at the top of return tank, be installed on check valve on the pipeline between device, device with
Pipeline is by flanged joint, it is characterised in that: thick oil pipeline is directly connected to thin oil surge tank entrance, and thin oil surge tank side, which is provided with, to be added
Material mouth is mixed diluent material stock tank with oil well time and is connect, and the outlet of thin oil surge tank is connect with thin oil heat exchanger；Thin oil heat exchanger it is dilute
Oil export is returned by thin oil to be mixed pump and transports to heavy oil wells bottom, the viscous crude outlet of thin oil heat exchanger be not dehydrated thick oil heat exchanger and connect；
The well liquid outlet for not being dehydrated thick oil heat exchanger is connect through flash column feed pump with flash column feed exchanger, and flash column charging is changed
Hot device is connect with flash column；The viscous crude outlet of flash column is connect through flash distillation column bottoms pump and flash column bottom heat exchanger with heating furnace；It dodges
The top exit for steaming tower connects flash column head space cooler, and flash column head space cooler is connect with flash column top heat exchanger；Flash tower top
Heat exchanger is connect with flash distillation tower buffer tank, and flash distillation tower buffer tank top exit is connect with heating furnace；Heating furnace and reaction tower
The viscous crude outlet of connection, reaction tower is connect with fractionating column；Fractionator overhead is connect with air cooler, and is connected and heated by pipeline
Furnace, tower bottom are viscous crude outlet；The viscous crude entrance of surge tank is set to the upper lateral part of tank body, and feed opening is set to tank body side, and outlet is set
In tank base；The entrance of thin oil heat exchanger is set to tank base, and thin oil outlet is set to top of the tank, and viscous crude outlet is set to tank body
Bottom, gas access set out tank body side；The top for not being dehydrated thick oil heat exchanger is equipped with viscous crude entrance, and tank body side is equipped with oil well
Liquid outlet, bottom are equipped with sewage draining exit；The top gas outlet of the flash column feed exchanger is connect with thin oil heat exchanger；Institute
The flash column feed exchanger heat transferring medium stated is communicated with flash column bottom heat exchanger heat transferring medium；The flash distillation tower buffer tank
Top gas outlet is connect with heating furnace；The air cooler is connect with fractionation return tank of top of the tower, at the top of fractionation return tank of top of the tower
Gas vent is connect with heating furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710344551.3A CN107355682B (en) | 2017-05-16 | 2017-05-16 | Heavy crude petroleum originates from certainly mixes diluent device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710344551.3A CN107355682B (en) | 2017-05-16 | 2017-05-16 | Heavy crude petroleum originates from certainly mixes diluent device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107355682A CN107355682A (en) | 2017-11-17 |
| CN107355682B true CN107355682B (en) | 2019-07-30 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710344551.3A Active CN107355682B (en) | 2017-05-16 | 2017-05-16 | Heavy crude petroleum originates from certainly mixes diluent device |
Country Status (1)
| Country | Link |
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| CN (1) | CN107355682B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201040747Y (en) * | 2007-03-30 | 2008-03-26 | 中国石油天然气股份有限公司 | Equipment combination for adjusting feeding temperature of ultra-thick crude oil delay coking fractionating tower |
| CN102234536A (en) * | 2010-05-07 | 2011-11-09 | 中国石油化工股份有限公司 | Combined technology for processing heavy oil |
| CN104673371A (en) * | 2013-12-02 | 2015-06-03 | 中石化洛阳工程有限公司 | Method for improving yield of delay coking liquid products |
| CN105754644A (en) * | 2014-12-17 | 2016-07-13 | 郭米慧 | Coal tar treatment system |
-
2017
- 2017-05-16 CN CN201710344551.3A patent/CN107355682B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201040747Y (en) * | 2007-03-30 | 2008-03-26 | 中国石油天然气股份有限公司 | Equipment combination for adjusting feeding temperature of ultra-thick crude oil delay coking fractionating tower |
| CN102234536A (en) * | 2010-05-07 | 2011-11-09 | 中国石油化工股份有限公司 | Combined technology for processing heavy oil |
| CN104673371A (en) * | 2013-12-02 | 2015-06-03 | 中石化洛阳工程有限公司 | Method for improving yield of delay coking liquid products |
| CN105754644A (en) * | 2014-12-17 | 2016-07-13 | 郭米慧 | Coal tar treatment system |
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| Publication number | Publication date |
|---|---|
| CN107355682A (en) | 2017-11-17 |
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Address after: 257091 Shandong Province, Dongying city the Yellow River Road No. 721 senuo Victory Mansion Patentee after: Suno Technology Co., Ltd Address before: 257091 Shandong Province, Dongying city the Yellow River Road No. 721 senuo Victory Mansion Patentee before: Shengli Oilfield Sino Shengli Engineering Co., Ltd. |
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