CN1570033A - Crude oil desalting method and device using rotational flow breakaway technology - Google Patents
Crude oil desalting method and device using rotational flow breakaway technology Download PDFInfo
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- CN1570033A CN1570033A CN 200410018202 CN200410018202A CN1570033A CN 1570033 A CN1570033 A CN 1570033A CN 200410018202 CN200410018202 CN 200410018202 CN 200410018202 A CN200410018202 A CN 200410018202A CN 1570033 A CN1570033 A CN 1570033A
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Abstract
The invention disclose a crude oil desalting method and device using rotational flow breakaway technology, wherein the method consists of, isolating the primary oil with charged water and demulsifying agent into oil phase and oil-contaminated water at 100-300 deg. C, isolating the oil phase through sedimentation by precipitation tank, entering downstream unit, charging the dirty oil into dirty oil tank, and discharging the salt-containing sewage water. One stage, two stage or multiple stage cyclone desalting unit can be utilized based on the requirement.
Description
Technical field
The present invention relates to a kind ofly remove the method and the device thereof of salt in the crude oil, can be widely used in the refining of petroleum field with cyclone technique.
Background technology
Crude oil contains salt and impurity, and this all has adverse influence for the processing of crude oil and equipment and product, all requires desalination before the refining.Along with the development of secondary processing technology in recent years; saltiness behind the crude oil desalting has also been proposed more specifically to require: if be purpose with anticorrosion; salt content of crude oil need be not more than 5mg/L after the desalination; if the protection secondary processing process catalyzer; then require advanced desalination; salt content of crude oil is not more than 3mg/L after the desalination, moisture being not more than to 0.3% (volume ratio).
Full scale plant normally utilizes electric desalting method or chemical desalting method to remove, though electric desalting technology uses comparative maturity, has that energy consumption is big, floor space big, the not high defective of desalting and dewatering rate.The saltiness of calendar year 2001 Sinopec system 52 cover electric desalting facility crude oil, average 34.29mg/L before taking off, the highest 280mg/L, minimum 1.58mg/L.One-level is taken off the average 11.1mg/L in back, the highest 45.4mg/L, minimum 1.56mg/L.Secondary takes off the average 3.54mg/L in back, the highest 12.6mg/L, minimum 0.16mg/L.Take off the back saltiness and be not more than 56% of the total electric desalting facility of accounting for of 3mg/L; That takes off back saltiness 3-5mg/L accounts for 24%; Take off the back saltiness and account for 17% greater than 5mg/L.As seen, the electric desalting general effect is unsatisfactory.
In recent years, lot of domestic and international units has been carried out the crude oil desalting research of non-electric desalting in succession, and major technology has centrifuging, filtration method, direct current hydrocyclone desalting etc., and these technology have obtained no small achievement, but do not see the industrialization achievement of making public.The cyclone separator volume is little, in light weight, processing speed is fast, is a kind of novel, efficient, energy-conservation separating device, can use it for dehydrating of crude oil production.The present invention adopts the method for cyclonic separation to remove salt and impurity in the crude oil, and develops a kind of new crude oil hydrocyclone desalting associated plant.
Summary of the invention
The objective of the invention is to propose a kind of method and device thereof that removes salt in the crude oil with cyclone separation process.Primary technical problem to be solved by this invention be overcome existing electric desalting equipment energy consumption big, take up an area of the new technology that shortcomings such as big and centrifuging, filtration method, direct current hydrocyclone desalting complicated operation provide a kind of crude oil desalting.Another technical problem to be solved by this invention provides special-purpose device in a kind of above-mentioned treatment process, and it is simple in structure, implements easily, invest little, easy to operate, and suitable long-term operation.
The present invention is achieved by the following technical solutions: utilizing one-level hydrocyclone desalting device (2-1) is oil phase and oily(waste)water with crude separation; Oily(waste)water advances slurry tank (3-3) and is separated into sump oil and saline sewage, and sump oil is arranged into slop oil tank, and saline sewage effluxes; Isolated oil phase enters secondary hydrocyclone desalting device (2-2) after injecting water and emulsion splitter, be oil phase and oily(waste)water through cyclonic separation again, oil phase advances slurry tank (3-1), the back crude oil that takes off that sedimentation goes out enters downstream unit, oily(waste)water and advance slurry tank (3-2) together from the oily(waste)water of secondary hydrocyclone desalting device (2-2), the sump oil that sedimentation goes out is arranged into slop oil tank, and saline sewage re-injection first step crude oil hydrocyclone desalting device and crude oil mix, and advance first step crude oil hydrocyclone desalting device 2
-1
Above-mentioned crude oil hydrocyclone desalting device adopts patent ZL00217613.0 cyclone separator structure, and by accompanying drawing 3 as seen, said crude oil desalting device comprises housing and cyclone pipe; Cyclone pipe shown in the accompanying drawing 4 comprises cylinder chamber section 13, big tapering chamber section 14, middle tapering chamber section 15, conelet degree chamber section 16, tailpipe section 17, upflow tube 18 and opening for feed 19; Housing is separated into three intervals, promptly collects light chamber, the heavy chamber of collection and feed cavity; Collect light chamber and be connected with upflow tube, the heavy chamber of collection is connected with tailpipe section, and feed cavity is connected with crude oil import;
Said housing is provided with crude oil import, oily(waste)water outlet and takes off the back crude exports, and is communicated with feed cavity, the heavy chamber of collection respectively and collects light chamber.Its cyclone pipe can a public feed cavity, an oil phase outlet plenum, an oily(waste)water outlet plenum, and feed cavity and outlet plenum can be three independent containers, also can be three parts in the container, to simplify the structure of production equipment.
The crude oil of annotating water enters feed cavity by the crude oil import on the said housing, tangentially inject cyclone pipe by opening for feed 10 then, by action of centrifugal force with bigger one the getting rid of mutually of proportion to the chamber wall, after tailpipe section is assembled, enter the heavy chamber of collection, discharge by the outlet of the oily(waste)water on the housing; The less phase of proportion then concentrates on the middle part of tube chamber, forms light phase core, enters the light chamber of collection, is discharged by the back crude exports of taking off on the housing at last, dewaters thereby finished from crude oil.As required, a plurality of cyclone pipes can be set in housing.
The water flow was 6% to 15% of a crude oil desalting device inlet flow rate when above-mentioned crude oil desalting device was operated, and was volume percent, to reach good separating effect.
The service temperature of hydrocyclone desalting device is at 100 ℃～300 ℃, 0.18～0.30Mpa falls in the pressure between device import of crude oil hydrocyclone desalting and the underflow opening, crude oil hydrocyclone desalting device water flow is 6% to 15% of an inlet flow rate, and the settling time of oil phase in slurry tank is 20～50 minutes
The technical scheme that another technical problem adopted that the present invention solves is: a kind of device of realizing above-mentioned treatment process comprises:
Injector (1) is for the crude oil that enters the hydrocyclone desalting device injects water and emulsion splitter;
An one-level hydrocyclone desalting device (2-1), being used for crude separation is oil phase and oily(waste)water, and slurry tank (3-3), sedimentation is from the oily(waste)water of one-level hydrocyclone desalting device (2-1);
A secondary hydrocyclone desalting device (2-2), with inject water and emulsion splitter, separate once more from one-level hydrocyclone desalting device (2-1) separated oil phase;
Be used for the slurry tank (3-1) of sedimentation from the oil phase of secondary hydrocyclone desalting device (2-2); Be used for the slurry tank (3-2) of sedimentation from the oily(waste)water of secondary hydrocyclone desalting device (2-2);
Slurry tank (3-2) is connected with one-level hydrocyclone desalting device (2-1) through injector (1).
Compared with prior art, the invention has the advantages that: overcome shortcomings such as the big and centrifuging of existing electric desalting equipment energy consumption, filtration method, direct current hydrocyclone desalting complicated operation.Production equipment is simple in structure, implements easily, invests for a short time, easy to operate, and suitable long-term operation is adapted at promoting the use of on the refining of petroleum industry.
Description of drawings
Accompanying drawing 1 is a crude oil hydrocyclone desalting device schema (one-level), wherein:
1-water filling mixing tank 2
-1Crude oil hydrocyclone desalting device 3
-1-slurry tank 3
-2-slurry tank;
Accompanying drawing 2 is a crude oil hydrocyclone desalting device schema (secondary)
1-water filling mixing tank 2
-1Crude oil hydrocyclone desalting device 2
-2Crude oil hydrocyclone desalting device 3
-1-slurry tank 3
-2-slurry tank, 3
-3-slurry tank;
Accompanying drawing 3 is a crude oil hydrocyclone desalting device structure iron, wherein:
4-takes off the back crude exports 5-tube sheet 6-cyclone pipe 7-tube sheet heavy chamber of the 8-collection light chamber of 9-collection 10-feed cavity 11-crude oil import 12-oily(waste)water outlet;
Accompanying drawing 4 is the cyclone pipe structure iron, wherein:
Tapering chamber section 16-conelet degree chamber section 17-tailpipe section 18-upflow tube 19-opening for feed among the big tapering chamber of the 13-cylinder chamber section 14-section 15-
Further illustrate content of the present invention below in conjunction with embodiment, but these examples do not limit protection scope of the present invention.
It is the benchmark operating mode that Shanghai Gaoqiao Petrochemical Company refinery crude oil reaches crude oil with outstanding promise, horse hila, Cabbeen.Operating mode I wherein: outstanding promise crude oil accounts for 50%, and horse hila crude oil accounts for 50%; Operating mode II:100% Cabbeen reaches crude oil.Density is about 0.860g/cm3, and water content is not between 0.09～0.15% (body) before the water filling, and swirler crude oil import temperature is 110 ℃.Crude oil desalting device intake pressure is 1.1Mpa, and the imported crude oil salts contg is not more than 8mg/L.
Viscosity of crude
| The crude oil kind | The horse hila | Cabbeen reaches | Jie Nuo |
| Viscosity (50 ℃) (mm 2.s -1) | ????9.466 | ????17.72 | ????11.27 |
Salts contg adopts conductometric titration to measure.Water-content adopts State Standard of the People's Republic of China GB/T 260-77 petroleum products aquametry to measure.
Embodiment one:
When crude oil hydrocyclone desalting device import salts contg is not more than 8mg/L, select one-level hydrocyclone desalting device for use, accompanying drawing 1 is seen in technical process.Crude oil hydrocyclone desalting device is oil phase and oily(waste)water at 100 ℃～300 ℃ crude separation that will annotate water, emulsion splitter.Oil phase is through slurry tank 3
-1Settlement separate for taking off back crude oil and oily(waste)water, take off back crude oil and enter downstream unit, oily(waste)water enters slurry tank 3
-2Oily(waste)water is through slurry tank 3
-2Settlement separate is sump oil and saline sewage, and sump oil advances slop oil tank, and saline sewage effluxes.
The hydrocyclone desalting system operating parameters:
Service temperature: 100 ℃～300 ℃.
Working pressure falls: 0.18～0.30Mpa falls in the pressure between device import of crude oil hydrocyclone desalting and the underflow opening.
Crude oil hydrocyclone desalting device water flow is 6% to 15% of an inlet flow rate.
Oil phase sedimentation 30 minutes in slurry tank.
Effect:
When crude oil hydrocyclone desalting device import salts contg was not more than 8mg/L, crude oil desalting device oil phase outlet crude oil desalting content was lower than 3mg/L, moisture 0.1% (volume ratio) of reducing to; The back crude oil desalting content that takes off after the slurry tank sedimentation is lower than 3mg/L, moisture 0.1% (volume ratio) of reducing to.Water-content adopts State Standard of the People's Republic of China GB/T 260-77 petroleum products aquametry to measure, and conductometric titration is adopted in the salts contg analysis.
Embodiment two:
Crude oil hydrocyclone desalting device import salts contg adopts secondary hydrocyclone desalting device during greater than 8mg/L, and accompanying drawing 2 is seen in technical process.Utilizing one-level hydrocyclone desalting device (2-1) is oil phase and oily(waste)water with crude separation; Oily(waste)water advances slurry tank (3-3) and is separated into sump oil and saline sewage, and sump oil is arranged into slop oil tank, and saline sewage effluxes; Isolated oil phase enters secondary hydrocyclone desalting device (2-2) after injecting water and emulsion splitter, be oil phase and oily(waste)water through cyclonic separation again, oil phase advances slurry tank (3-1), the back crude oil that takes off that sedimentation goes out enters downstream unit, oily(waste)water and advance slurry tank (3-2) together from the oily(waste)water of secondary hydrocyclone desalting device (2-2), the sump oil that sedimentation goes out is arranged into slop oil tank, and saline sewage re-injection first step crude oil hydrocyclone desalting device and crude oil mix, and advance first step crude oil hydrocyclone desalting device 2
-1
The service temperature of hydrocyclone desalting device is at 100 ℃～300 ℃, 0.18～0.30Mpa falls in the pressure between device import of crude oil hydrocyclone desalting and the underflow opening, crude oil hydrocyclone desalting device water flow is 6% to 15% of an inlet flow rate, and the settling time of oil phase in slurry tank is 30 minutes.
During the little 15mg/L of crude oil hydrocyclone desalting device import salts contg, secondary crude oil hydrocyclone desalting device oil phase outlet crude oil desalting content is lower than 3mg/L, moisture 0.3% (volume ratio) of reducing to; The back crude oil desalting content that takes off after the slurry tank sedimentation is lower than 3mg/L, moisture 0.1% (volume ratio) of reducing to.Water-content adopts State Standard of the People's Republic of China GB/T 260-77 petroleum products aquametry to measure, and conductometric titration is adopted in the salts contg analysis.
But the actual saltiness of above-mentioned technology based on crude determines to adopt one-level, secondary or multistage hydrocyclone desalting device to separate, and determines oil phase and the oily(waste)water settling time in slurry tank according to required separating effect, in the hope of reaching ideal effect.
Claims (8)
1, a kind of method of utilizing cyclone separation process to carry out crude oil desalting is characterized in that, under 100 ℃～300 ℃, utilizing one-level hydrocyclone desalting device (2-1) is oil phase and oily(waste)water with crude separation; Oily(waste)water advances slurry tank (3-3) and is separated into sump oil and saline sewage, and sump oil is arranged into slop oil tank, and saline sewage effluxes; Isolated oil phase enters secondary hydrocyclone desalting device (2-2) after injecting water and emulsion splitter, be oil phase and oily(waste)water through cyclonic separation again, oil phase advances slurry tank (3-1), the back crude oil that takes off that sedimentation goes out enters downstream unit, oily(waste)water and advance slurry tank (3-2) together from the oily(waste)water of secondary hydrocyclone desalting device (2-2), the sump oil that sedimentation goes out is arranged into slop oil tank, water with enter one-level hydrocyclone desalting device (2-1) once more after crude oil mixes.
2, crude oil desalting method as claimed in claim 1 is characterized in that, the service temperature of hydrocyclone desalting device is 100～300 ℃.
3, crude oil desalting method as claimed in claim 1 is characterized in that, the import of hydrocyclone desalting device and the pressure between underflow opening are reduced to 0.18～0.30Mpa.
4, crude oil desalting method as claimed in claim 1 is characterized in that, the water flow of hydrocyclone desalting device is 6%～15% of an inlet flow rate.
5, crude oil desalting method as claimed in claim 1 is characterized in that, through the sedimentation 20～50 minutes in slurry tank of crude oil hydrocyclone desalting device separated oil phase.
6, crude oil desalting method as claimed in claim 1 is characterized in that, the water content in crude oil volume ratio is 5～10% after the water filling.
7, crude oil desalting method as claimed in claim 5 is characterized in that, through the sedimentation 30 minutes in slurry tank of crude oil hydrocyclone desalting device separated oil phase.
8, a kind of device of implementing the described method of claim 1 is characterized in that, comprising: injector (1), for the crude oil that enters the hydrocyclone desalting device injects water and emulsion splitter;
An one-level hydrocyclone desalting device (2-1), being used for crude separation is oil phase and oily(waste)water, and slurry tank (3-3), sedimentation is from the oily(waste)water of one-level hydrocyclone desalting device (2-1);
A secondary hydrocyclone desalting device (2-2), with inject water and emulsion splitter, separate once more from one-level hydrocyclone desalting device (2-1) separated oil phase;
Be used for the slurry tank (3-1) of sedimentation from the oil phase of secondary hydrocyclone desalting device (2-2); Be used for the slurry tank (3-2) of sedimentation from the oily(waste)water of secondary hydrocyclone desalting device (2-2);
Slurry tank (3-2) is connected with one-level hydrocyclone desalting device (2-1) through injector (1).
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| CN 200410018202 CN1219856C (en) | 2004-05-10 | 2004-05-10 | Crude oil desalting method and device using rotational flow breakaway technology |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101139107B (en) * | 2007-08-16 | 2010-08-11 | 华东理工大学 | Slag included lime cream slag removing method and device |
| CN102424444A (en) * | 2011-10-25 | 2012-04-25 | 华东理工大学 | Method and device for removing oil from desalted water of crude electrostatic desalting apparatus |
| CN103224807A (en) * | 2013-05-10 | 2013-07-31 | 中国石油大学(华东) | Process for carrying out complextion and denitrification on coker gas oil |
| CN103396830A (en) * | 2013-08-14 | 2013-11-20 | 中国石油大学(华东) | Device and method for dehydrating heavy sump oil |
| CN109135819A (en) * | 2018-10-19 | 2019-01-04 | 中石化南京工程有限公司 | A kind of system and method handling oil well crude oil |
| CN109399888A (en) * | 2017-08-15 | 2019-03-01 | 中国石油化工股份有限公司 | The continuous desalting and dewatering method and apparatus of oily sludge |
| CN112588461A (en) * | 2020-11-26 | 2021-04-02 | 东北石油大学 | Multi-stage cluster cyclone separation device for oil-water separation |
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- 2004-05-10 CN CN 200410018202 patent/CN1219856C/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101139107B (en) * | 2007-08-16 | 2010-08-11 | 华东理工大学 | Slag included lime cream slag removing method and device |
| CN102424444A (en) * | 2011-10-25 | 2012-04-25 | 华东理工大学 | Method and device for removing oil from desalted water of crude electrostatic desalting apparatus |
| CN102424444B (en) * | 2011-10-25 | 2013-06-12 | 华东理工大学 | Method and device for removing oil from desalted water of crude electrostatic desalting apparatus |
| CN103224807A (en) * | 2013-05-10 | 2013-07-31 | 中国石油大学(华东) | Process for carrying out complextion and denitrification on coker gas oil |
| CN103396830A (en) * | 2013-08-14 | 2013-11-20 | 中国石油大学(华东) | Device and method for dehydrating heavy sump oil |
| CN103396830B (en) * | 2013-08-14 | 2015-05-20 | 中国石油大学(华东) | Device and method for dehydrating heavy sump oil |
| CN109399888A (en) * | 2017-08-15 | 2019-03-01 | 中国石油化工股份有限公司 | The continuous desalting and dewatering method and apparatus of oily sludge |
| CN109399888B (en) * | 2017-08-15 | 2021-12-17 | 中国石油化工股份有限公司 | Method and device for continuous desalting and dewatering of oily sludge |
| CN109135819A (en) * | 2018-10-19 | 2019-01-04 | 中石化南京工程有限公司 | A kind of system and method handling oil well crude oil |
| CN109135819B (en) * | 2018-10-19 | 2021-05-11 | 中石化南京工程有限公司 | System and method for treating crude oil of oil well |
| CN112588461A (en) * | 2020-11-26 | 2021-04-02 | 东北石油大学 | Multi-stage cluster cyclone separation device for oil-water separation |
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|---|---|
| CN1219856C (en) | 2005-09-21 |
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