CN105623706B - Crude oil continuous still dewatering - Google Patents
Crude oil continuous still dewatering Download PDFInfo
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- CN105623706B CN105623706B CN201410584023.1A CN201410584023A CN105623706B CN 105623706 B CN105623706 B CN 105623706B CN 201410584023 A CN201410584023 A CN 201410584023A CN 105623706 B CN105623706 B CN 105623706B
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Abstract
The invention discloses a kind of crude oil continuous still dewatering.The dewatering includes continuously being passed through wet crude into the feed duct line that crude oil continuous still dehydration device feeds conveying assembly, the pre-add hot pipeline entered back into preheating component is preheated, distilled subsequently into the housing in housing unit, water and light oil in crude oil are discharged from housing upper gaseous phase outlet, enter light oil and water storage tank after reclaiming component condensation through distillation gas, water therein is discharged from light oil and water storage tank bottom, and carburet hydrogen is discharged into carburet hydrogen recycling can from light oil and water storage tank top；Heavy oil in crude oil is discharged from lower housing portion liquid-phase outlet, enters heavy oil recycling can after reclaiming component condensation through heavy oil.Pre-add heat treatment is carried out by treating dehydrated material (such as crude oil) on pre-add hot pipeline, then will carry out distilling in housing unit by the material to be drained off heated while vapor-liquid separation is to realize dehydration.
Description
Technical field
The present invention relates to oil product distillation dehydration method, in particular it relates to a kind of crude distillation dewatering.
Background technology
For crude oil evaluation and analysis of oil, the presence of sample reclaimed water can have directly to the analysis detection project of sample
Influence, such as density, flash-point, boiling range, viscosity, ash content, carbon residue, condensation point, metal, therefore aqueous crude oil and oil product are being carried out
Evaluate, analysis must be dehydrated before detecting.
At present, have a variety of in the method that crude oil is dehydrated in use for laboratory, including deposition dehydrating method, autoclave evaporation, electricity
Evaporation, microwave dehydration method and distillation dehydration method etc..Wherein distillation dehydration method is by steaming water vapor oil product heating, reaching
To the purpose of oil dehydrating.This method almost can all take off the water in oil product, and it is external to be not required to addition demulsifier etc.
Reagent, is compared with other dewatering, be dehydrated it is more complete, simple and easy to do, do not influence oil product component the features such as, so non-
Often it is adapted to apply in laboratory in crude oil evaluation, analysis of oil.
The common distillation dehydration method in current laboratory, is typically that raw material is distilled in a fixed distillation still,
And then cause crude oil in moisture evaporation, with realize crude oil dehydration purpose.It is to be added to crude oil in fixed distillation still, leads to
Heating distillation still is crossed, so that moisture evaporation and then dehydration, common device include：For example in the U of Chinese patent CN 202606174
In give a kind of crude oil dewatering instrument, a kind of way of distillation oil dehydrating plant is given in the U of Chinese patent CN 202912907
Deng.
Existing this distillation dehydration method, on the one hand due to being limited to by device volume, the dewatered oil obtained every time
Amount it is limited, larger amount of dewatered oil is obtained if desired, then is needed to repeat repeatedly, is not only consumed energy but also time-consuming.Separately
On the one hand due to the crude oil in distillation still, with the volatilization of moisture, water content is gradually decreased, and for moisture reduction
Requirement of the crude oil to vapo(u)rizing temperature then more and more higher, in order to obtain the satisfactory crude oil of dehydration rate, then need extension to be dehydrated
Time, increase dehydration temperaturre.
The content of the invention
It is continuous quick de- can be carried out to crude oil it is an object of the invention to provide a kind of crude oil continuous still dewatering
Water, crude charging capacity is big, and dehydration temperaturre is low, and controllable continuous feed flow velocity.
The invention provides a kind of crude oil continuous still dewatering, this method includes wet crude being continuously passed through original
Oily continuous still dehydration device feeds the feed duct line of conveying assembly, and the pre-add hot pipeline entered back into preheating component enters
Row preheating, is distilled subsequently into the housing in housing unit, and the water and light oil in crude oil are from housing upper gaseous phase outlet
Discharge, enters light oil and water storage tank after reclaiming component condensation through distillation gas, water therein is discharged from light oil and water storage tank bottom, gas
Body hydrocarbon is discharged into carburet hydrogen recycling can from light oil and water storage tank top；Heavy oil in crude oil is arranged from lower housing portion liquid-phase outlet
Go out, enter heavy oil recycling can after reclaiming component condensation through heavy oil.
Above-mentioned crude oil continuous still dewatering, dehydrated material (such as crude oil) is treated on pre-add hot pipeline and is carried out in advance
Heat, then will carry out distilling in housing unit by the material to be drained off heated while vapor-liquid separation is to realize
Dehydration.This method has preferable operability, and inlet amount can be adjusted as needed, and continuous feed is former to obtain dehydration
Oil, continuous feed and discharging are conducive to shortening residence time of the material in distillation dehydration device, it is to avoid crude oil is in dehydration
Thermally decomposed, crude oil after dehydration is remained in that original property is constant.
Meanwhile, above-mentioned crude oil continuous still dewatering is due to being preheated material in pre-add hot pipeline, in advance
Heating process makes light component in material and water, in order to material enter in housing unit become in space it is big in the case of it is fast
Speed distillation carries out gas-liquid separation, advantageously reduces vapo(u)rizing temperature, energy consumption, and the moisture preferably in abjection crude oil.
Other features and advantages of the present invention will be described in detail in subsequent embodiment part.
Brief description of the drawings
Accompanying drawing is, for providing a further understanding of the present invention, and to constitute a part for specification, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.
Fig. 1 is the structural representation of the crude oil continuous still dehydration device used of the inventive method.
Description of reference numerals
The housing upper of 11 housing unit 111
The upper cover of 112 lower housing portion 113
114 low heads
The upper heater of 12 primary heater 121
122 lower heaters
The 20 preheating pre-add hot pipelines of component 21
The plug at end part head of 22 secondary heater 23
The 30 charging feed-lines of conveying assembly 31
The feed-line of 311 feeding line 312
The leakage fluid dram of 313 tapping valve 314
The controllable temperature feed pump of 32 the 3rd heater 33
40 heavy oil reclaim the cooling component of component 41 first
The outer tube of 411 inner tube 412
The heavy oil recycling can of 413 temperature-reducing medium flowing lumen 42
The oil discharge outlet of 421 draining valve 422
50 distillation gas reclaim the cooling component of component 51 second
52 light oil and the draining valve of water storage tank 521
The carburet hydrogen recycling can of 522 discharge outlet 53
The air bleeding valve of 531 intake valve 532
533 exhaust outlets
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
In the present invention, term " heavy oil " and term " light oil " are relative concept.Wherein " heavy oil " refers to de- in distillation
During water, boiling point is more than 300 DEG C of cut, and " light oil " refers to that being not more than 300 DEG C in distillation dehydration process mid-boiling point evaporates
Point, carburet hydrogen is C3~C4 hydrocarbon.If containing carburet hydrogen in crude oil, the top for carrying the housing from housing unit by light oil is arranged
Go out.
Inventor proposes a kind of crude oil continuous still dewatering.As shown in figure 1, this method include will be aqueous
Crude oil is continuously passed through the feed duct line 31 that crude oil continuous still dehydration device feeds conveying assembly 30, enters back into preheating
Pre-add hot pipeline 21 in component 20 is preheated, and is distilled subsequently into the housing in housing unit 11, in crude oil
Water and light oil are discharged from housing upper gaseous phase outlet, are reclaimed through distillation gas after component 50 is condensed and are entered light oil and water storage tank 52, its
In water discharged from light oil and the bottom of water storage tank 52, carburet hydrogen is discharged into carburet hydrogen recycling can from light oil and the top of water storage tank 52
53；Heavy oil in crude oil is discharged from lower housing portion liquid-phase outlet, is reclaimed through heavy oil after component 40 is condensed and is entered heavy oil recycling can 42.
Above-mentioned crude oil continuous still dewatering, is entered by treating dehydrated material (such as crude oil) on pre-add hot pipeline
Row pre-add is heat-treated, then by vapor-liquid separation while distillation by the material to be drained off heated in housing unit
To realize dehydration.This method has preferable operability, and inlet amount can be adjusted as needed, and continuous feed is de- to obtain
Water crude oil, continuous feed and discharging are conducive to shortening residence time of the material in the de- device of distillation, it is to avoid crude oil is in dehydration
In thermally decomposed, make after dehydration the crude oil original property of holding of trying one's best constant.
Meanwhile, above-mentioned crude oil continuous still dewatering, due to being preheated material in pre-add hot pipeline, in advance
Heating process makes light component in material and water, in order to material enter in housing unit become in space it is big in the case of it is fast
Speed distillation carries out gas-liquid separation, advantageously reduces vapo(u)rizing temperature, energy consumption, and the quickly moisture in abjection crude oil.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, charging conveying assembly 30 includes：The heater 32 of feed duct line 31 and the 3rd.Feed duct line 31
End with preheating component 20 in pre-add hot pipeline 21 be connected；3rd heater 32 is used to adjust the feed duct line
Temperature inside 31.
Temperature in conveying assembly 30 is fed in practical operation should be less than the temperature in preheating component 20, due in heating
There is provided charging conveying assembly 30 is treated dehydrated material and tentatively heated before component 20 so that the temperature of material to be drained off is carried
Rise, it is easy to flow into preheating component 20 and heated.When now material inflow heating component 20 is heated, the temperature of required heating
Difference is relatively small, can shorten the length of conveying pipeline in heating component 20, to reduce the energy consumption that longer conveying pipeline is brought
Loss.
In the preferred embodiment of the present invention, wet crude is continuously passed through to crude oil continuous still dehydration device
During, control above-mentioned 3rd heater 32 with by heating crude oil to 20~100 DEG C, to promote crude oil to be tentatively heated.It is preferred that
Ground, above-mentioned 3rd heater 32 can be multiple heating members being distributed on feed duct line 31, it is highly preferred that the 3rd heating
Device 32 is the 3rd heating mantle for being wrapped in the periphery of feeding line 31.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, also include controllable temperature feed pump 33 in charging conveying assembly 30, controllable temperature feed pump 33 is arranged on charging
On feed-line 31.This controllable temperature feed pump 33 may advantageously facilitate similar to this treating for dope under normal temperature of crude oil
Dehydrated material is readily flowed after heated, and then the continuous feed amount of controllable material to be drained off.By taking crude oil as an example, in actual behaviour
Can be with the condensation point of based on crude and viscosity temperature, 20~100 DEG C of controllable temperature feed pump temperature control scope in work.
Preferably, in crude oil continuous still dehydration device used in above-mentioned crude oil continuous still dewatering of the invention
In, feed duct line 31 includes feeding line 311 and feed-line 312.Wet crude from feeding line 311 continuously into
The crude oil continuous still dehydration device.Wherein, feeding line 311 is provided with positioned at the feed(raw material)inlet on top, positioned at bottom
Tapping valve 313 and leakage fluid dram 314, and superposed controllable temperature feed pump 33；The one end of feed-line 312 is connected to feed pipe
On line 311, and positioned between controllable temperature feed pump 33 and tapping valve 313, the other end is connected on pre-add hot pipeline 21.
Using the crude oil continuous still dehydration device with this structure, by feed duct line, 31 points are feeding line
311 and feed-line 312, be on the one hand conducive to the charging of material to be drained off, particularly with the material to be drained off of thick presence
Charging, on the other hand, be easy to the cleaning after the distillation dehydration end of job, by by positioned at the bottom of feeding line 311
Tapping valve 313 is opened, you can so that cleaning fluid is discharged by feeding line 311 and feed-line 312 simultaneously.Meanwhile, in feed pipe
The bottom of line 311 sets tapping valve 313, can be also used for after continuous still dehydrator is cleaned with solvent, and residual is molten in blow-down pipe
Agent, is passed through nitrogen purging instrument.
Preferably, the draw ratio of above-mentioned feed duct line 31 is 10~300.Feed duct line 31 in the present invention
Draw ratio is not limited to above range, is disposed in above range to have and causes material to be drained off is heated to be more uniformly distributed, and
Dehydrating effect more preferably effect.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, preheating component 20 includes：Pre-add hot pipeline 21 and secondary heater 22.Pre-add hot pipeline 21 and housing
Arrival end positioned at middle part is connected.Secondary heater 22 is used to adjust the temperature inside pre-add hot pipeline 21.It is above-mentioned in the present invention
In crude oil continuous still dehydration device used in above-mentioned crude oil continuous still dewatering, do not have for secondary heater 22
Particular/special requirement, as long as the requirement of adjustment temperature can be realized, such as secondary heater 22 can multiple be distributed in pre-add
Heating member on hot pipeline 21.Secondary heater 22 is to be wrapped in pre-add hot pipeline in the preferred embodiment of the present invention
Second heating mantle of 21 peripheries.Heating mantle can be more complete the periphery for being wrapped in material to be heated so that heating-up temperature is more equal
It is even.
Preferably, in above-mentioned crude oil continuous still dewatering, wet crude is continuously passed through to crude oil continuous still
During dehydration device, the temperature for controlling secondary heater is 100~300 DEG C.The temperature of secondary heater in the present invention
Above range is not limited to, is above range by its limit temperature, is conducive to making material (aqueous original on pre-add hot pipeline 21
Oil) in light component and water, in order to material enter in housing unit become in space it is big in the case of rapid distillation carry out
Gas-liquid separation, advantageously reduces vapo(u)rizing temperature, energy consumption, and the moisture preferably in abjection crude oil.
Preferably, in crude oil continuous still dehydration device used in above-mentioned crude oil continuous still dewatering of the invention
In, the draw ratio of pre-add hot pipeline 21 is 2~30, more preferably 10~20.The draw ratio of pre-add hot pipeline 21 is simultaneously in the present invention
Above range is not limited to, being disposed in above range has so that material to be drained off is more susceptible to thermal evaporation, to improve dehydration
Efficiency.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, housing unit 11 includes：Housing, upper cover 113 and low head 114.Housing central section is provided with arrival end, on
Portion sets gaseous phase outlet, bottom and sets liquid-phase outlet；The open top of upper cover 113 and housing is tightly connected；Low head 114 and housing
Bottom opening be tightly connected.Wherein preferred gaseous phase outlet is set close to upper cover 113, and preferred liquid phase outlet is close to low head
114 are set, and arrival end is located between gaseous phase outlet and liquid-phase outlet.This housing unit 11 sets upper cover 113 and low head
114 also help its disassembly, cleaning and replacing, and then are conducive to extending the service life of housing unit 11.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, housing unit 11 is provided with primary heater 12, and primary heater 12 is used to adjust the enclosure interior
Temperature.
Do not have particular/special requirement for primary heater 12 in the present invention, as long as the requirement of adjustment temperature can be realized i.e.
Can, such as primary heater 12 can be the heating coil for being arranged on enclosure interior, in a kind of preferred embodiment of the present invention
Middle primary heater 12 is the first heating mantle for being wrapped in housing periphery in housing unit 11, the parcel that heating mantle can be more complete
In the periphery of material to be heated so that heating-up temperature is more uniformly distributed.
Above-mentioned housing is preferably gas-liquid separation post, when heat-treated material to be drained off enters the housing of housing unit 11
When, begin to carry out vapor-liquid separation, gas flows to gaseous phase outlet above, and liquid is to underlying liquid-phase outlet
Flowing.By setting primary heater 12 that the temperature of enclosure interior is adjusted, be conducive to promoting in flow regime
Material further distills, and then improves dehydration rate.
Preferably, in crude oil continuous still dehydration device used in above-mentioned crude oil continuous still dewatering of the invention
In, 21 middle part preferably with housing in housing unit 11 of preheating expects pipe line is connected, and by housing unit, 11 points are housing upper 111
With lower housing portion 112.Now, primary heater 12 includes upper heater 121 and lower heater 122.Upper heater 121 is used to adjust
The internal temperature of whole housing upper 111；Lower heater 122 is used for the internal temperature for adjusting lower housing portion 112.
In practical operation, it can cause upper heater 121 is identical with the temperature of secondary heater 22 (for example to enter to crude oil
During row dehydration, the temperature of upper heater 121 and secondary heater 22 is 100~300 DEG C), preferably make the temperature of lower heater 122
Higher than upper heater temperature (such as when being dehydrated to crude oil, temperature of the temperature than upper heater 121 of lower heater 122
Spend high 10~50 DEG C).By adjusting the temperature of upper heater and lower heater, it on the one hand can promote to flow downwardly into lower housing portion
112 liquid further carries out distillation dehydration, can on the other hand in view of the temperature difference between housing upper 111 and lower housing portion 112
Promote light hydrocarbon and water to be easier to flow up, and then promote the progress of dehydration by evaporation.
Preferably, the ratio of height to diameter of housing cavity is 5~60, preferably 10~30 in above-mentioned housing unit 11.In actual behaviour
, can be according to the quantity of heating component in above-mentioned continuous still dehydrator in work, the height of housing cavity in adjustment housing unit 11
Footpath ratio, to promote material heating to be drained off to be more uniformly distributed, dehydrating effect is more preferably.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, pre-add hot pipeline 21 is extended downwardly and housing inlet port end phase with deviateing 5 °~30 ° directions of horizontal plane
Even.Using this pipeline tilted down, be conducive to promoting it is heat-treated after material to be drained off flow into housing.More
Preferably, there is cleaning to be open for the one end of pre-add hot pipeline 21 away from housing, and the end being tightly connected with cleaning opening is sealed
Plug 23.
Preferably, the internal diameter of above-mentioned pre-add hot pipeline 21 is more than the internal diameter of feed duct line 31, more preferably pre-add heat pipe
The internal diameter of line 21 is 2~10 times of the internal diameter of feed duct line 31.On the one hand this structure is conducive to adaptation heating to treat
The pressure change of dehydrated material, improve processing safety, be on the other hand conducive to it is heat-treated after material to be drained off it is quick
Smoothly it is flowed into the housing in housing unit 11.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, preheating component 20 can be multigroup, and charging conveying assembly 30 is to be corresponded with preheating component 20
Multigroup, preferably 2-5 groups, such as 2 groups, 3 groups, 4 groups or 5 groups.Multigroup preheating component 20 and multigroup charging conveying assembly 30
Setting be more suitable for requirement of the industrialized production to equipment.In practical operation, each group can be preheated into group as needed
Part 20 is circumferentially connected with the housing in housing unit 11 respectively, or respectively in different height and the housing unit 11
Housing is connected., can be with for each group is preheated into the device that is circumferentially connected respectively with the housing in housing unit 11 of component 20
For carrying out running to multigroup material simultaneously, timeliness is improved.For each group is preheated into component 20 respectively in different height and shell
The connected device of housing in body component 11, can select the inflow being more suitable for according to the difference of material water ratio, can also be by
The different material of moisture content carries out distillation dehydration processing simultaneously.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, distillation gas, which reclaims component 50, to be included：Second cooling component and 51, light oil and water storage tank 52 and carburet hydrogen are returned
Closed cans 53.Second cooling one end of component 51 is connected with the gaseous phase outlet of the housing of housing unit 11；Light oil and water storage tank 52 and second
The other end of cooling component 51 is connected, and light oil and water storage tank 52 are provided with gaseous phase outlet；Carburet hydrogen recycling can 53 and light oil and
The gaseous phase outlet of water storage tank 52 is connected.
Component 50 is reclaimed by using this distillation gas, by light oil and Water Sproading and is separated.By the second cooling component 51
Admixture of gas cooled, being delivered to light oil and water storage tank 52, (periphery of the preferably distillation water storage tank 52 is formed with vacuum clip
Layer), then the light oil and water that are in a liquid state in light oil and water storage tank 52 are separated, carburet hydrogen is delivered in carburet hydrogen recycling can 53 and light
Oil separation.
Preferably, in above-mentioned crude oil continuous still dewatering of the invention, using distillation gas reclaim component 50 condense from
During water and light oil in the crude oil of housing upper gaseous phase outlet discharge, control second cools component 51 and light oil and water storage tank 52
Temperature be 1 DEG C~15 DEG C, the temperature of carburet hydrogen recycling can 53 is -80~-100 DEG C.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, heavy oil, which reclaims component, includes the first cooling component 41 and heavy oil recycling can 42.First cooling component 41 1
End is connected with the liquid-phase outlet of the housing in housing unit 11；The other end phase of heavy oil recycling can 42 and the first cooling component 41
Even.It is simple and operational stronger that this heavy oil reclaims modular construction.In practical operation, by the weight of the first cooling component 41
Oil is cooled to be reclaimed using heavy oil recycling can 42.
Preferably, in above-mentioned crude oil continuous still dewatering of the invention, component 40 is reclaimed using heavy oil and condensed from shell
When body lower liquid phase exports the heavy oil in the crude oil of discharge, the temperature for controlling the first cooling component 41 and heavy oil recycling can 42 is 20
~100 DEG C.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, the first cooling cooling of component 41 and second structure of component 51 does not have specific limitation, as long as can enter
Row cooling.In the preferred embodiment of the present invention, the above-mentioned first cooling component 41 and second cooling knot of component 51
Structure is identical, by taking the first cooling component 41 as an example, and the first cooling component 41 includes inner tube 411 and outer tube 412.The one end of inner tube 411
It is connected with the liquid-phase outlet of the housing in the housing unit 11, the other end is connected with heavy oil recycling can 42；Outer tube 412 is wrapped in
The periphery of inner tube 411, forms temperature-reducing medium flowing lumen 413 between outer tube 412 and inner tube 411.
This cooling modular construction, it is not only simple in construction, easily make, and also its cooling-down effect is more uniform.When by its
During applied to laboratory equipment, it can make to observe using glass material.Preferably wherein inner tube 411 is along material stream
Dynamic direction is with respect to the horizontal plane tilted down, and this structure tilted down is conducive to liquid in inner tube 411 to discharge.In actual behaviour
In work, temperature-reducing medium is passed into temperature-reducing medium flowing lumen 413, this preferred cooling water of temperature-reducing medium.
In the preferred embodiment of the present invention, crude oil used in above-mentioned crude oil continuous still dewatering is continuous
In distillation dehydration device, the bottom of heavy oil recycling can is provided with draining valve 421 and oil discharge outlet 422, in order to the discharge of heavy oil, light oil
Draining valve 521 and discharge outlet 522 are provided with the bottom of water storage tank, in order to the discharge of distilled water；The top of carburet hydrogen recycling can
Provided with air bleeding valve 532 and exhaust outlet 533, so as to fixed gas in device, the discharge of nitrogen used in during such as cleaning.
Beneficial effects of the present invention are further illustrated below with reference to specific embodiment.
(1) equipment that following examples are used is as shown in figure 1, concrete structure is as follows：
Continuous still dehydrator includes in crude oil continuous still dehydration device：Housing unit 11, primary heater 12, pre-add
Hot component 20, charging conveying assembly 30.Wherein housing unit 11 includes the gas-liquid separation post (Gao Jing of gas-liquid separation post enclosure interior
Sealed than the upper cover 113 20), with the open top of gas-liquid separation post to be tightly connected and with the bottom opening of gas-liquid separation post
The low head 114 of connection.Primary heater (the first heating mantle) 12 is wrapped in gas-liquid separation post periphery.Preheating component 20 includes
Pre-add hot pipeline 21 (draw ratio is 10) and the secondary heater (the second heating mantle) 22 for being wrapped in the periphery of pre-add hot pipeline 21.In advance
10 ° of directions of the heating deviation horizontal plane of pipeline 21, which extend downwardly to be connected with the middle part of gas-liquid separator 10, is classified as housing upper
111 and lower housing portion 112.Primary heater (the first heating mantle) 12 includes being used to adjust the temperature inside housing upper 111
Upper heater 121 and the lower heater 122 for adjusting the temperature inside lower housing portion 112.Charging conveying assembly 30 is arranged on
The upstream of component 20 is preheated, including (draw ratio of feed duct line 31 is 100, pre-add hot pipeline 21 to feed duct line 31
With the internal diameter ratio of feed duct line 31 5) and to be wrapped in the 3rd heater (the 3rd heating mantle) 32 of its periphery.Wherein feed
Feed-line 31 includes feeding line 311 and the feed-line 312 being connected between feeding line 311 and pre-add hot pipeline 21.
The top of feeding line 311 is provided with feed(raw material)inlet, and bottom is provided with tapping valve 313 and leakage fluid dram 314, in feed(raw material)inlet and tapping valve
Controllable temperature feed pump 33 is provided between 313.
Crude oil continuous still dehydration device：Including above-mentioned continuous still dehydrator, and with gas in continuous still dehydrator
The distillation gas recovery that the connected heavy oil of the liquid-phase outlet of liquid splitter reclaims component 40, is connected with the gaseous phase outlet of gas-liquid separation post
Component 50.Heavy oil recovery component 40 includes the first cooling component 41 being connected with the liquid-phase outlet of gas-liquid separation post and dropped with first
The connected heavy oil recycling can of warm component 41.The liquid-phase outlet that first cooling component 41 includes being connected to gas-liquid separation post is returned with heavy oil
Inner tube between closed cans 42, and it is wrapped in the outer tube 412 of the periphery of said inner tube 411, shape between outer tube 412 and inner tube 411
Into temperature-reducing medium flowing lumen 413.The bottom of heavy oil recycling can is provided with draining valve 421 and oil discharge outlet 422.Distillation gas reclaims component 50
Including the second cooling component 51, light oil and water storage tank 52 and the carburet hydrogen recycling can 53 being sequentially connected.Wherein second cooling component
51 is identical with the first cooling structure of component 41, and the bottom of light oil and water storage tank 52 is provided with draining valve 521 and discharge outlet 522, gas
The top of hydrocarbon recycling can is provided with air bleeding valve 532 and exhaust outlet 533.
(2) by taking crude oil as an example, the application method of above-mentioned crude oil continuous still dehydration device is illustrated.
Power-on, the condensation point and viscosity of based on crude set the temperature of the heater 32 of controllable temperature feed pump 33 and the 3rd as
1 DEG C to 80 DEG C, it is 0.5-2 ls/h to control crude oil flow velocity.The temperature of secondary heater 22 and upper heater 121 is set as 120
DEG C to 260 DEG C, the temperature of lower heater 122 is 150 DEG C to 300 DEG C.Set the second cooling component 51, light oil and water storage tank 52
Temperature is 1-15 DEG C, 20 DEG C to 100 DEG C of the temperature of the cooling component 41 of setting first.If crude oil is lighter, contain the gas such as carbon 3, carbon 4
Body, the chilling temperature that carburet hydrogen recycling can 53 need to be controlled in advance is -80 DEG C to -90 DEG C.After about 10 minutes, the temperature of instrument setting
Reach setting value, start controllable temperature feed pump 33, crude oil is sequentially passed through after charging conveying assembly, preheating component heated,
Flow into gas-liquid separation post.Separation, the water and oil of gasification are distilled in gas-liquid separation post reclaimed water and light oil constituents and heavy oil component
Gas rises to gaseous phase outlet on gas-liquid separation post and entered after the second cooling component 51, is cooled into liquid, flows into light oil and water
In collecting tank 52, in the carburet hydrogen recycling can 53 of -80 DEG C to -90 DEG C of carburet hydrogen entrance therein.Non- gas in gas-liquid separation post
The heavy oil of change flows to gas-liquid separation post bottom liquid-phase outlet, is flowed into after the second cooling component 41 in heavy oil recycling can 42.When even
Crude oil sample after continuous distillation dehydration is reached after the amount of demand, stops dehydration.Moisture is released from light oil and the bottom of water storage tank 52, will be light
Light oil is mixed with heavy oil in heavy oil recycling can 42 in oil and water storage tank 52, is used as dewatered oil sample.
Crude oil sample after dehydration determines water content by the detecting crude oil water content methods of GB/T 8929, if water content is less than
The water content of crude oil evaluation requires (0.3 mass %), terminates crude oil dehydration.If water content will higher than the water content of crude oil evaluation
(0.3 mass %) is asked, the dewatered oil of collection is reentered into controllable temperature feed pump 33 carries out distillation dehydration again, until water contains
Amount is required untill (0.3%) less than the water content of crude oil evaluation.
(3) water content, the measurement of crude oil dehydration rate, the computational methods of crude oil are as follows after the water content of crude oil, dehydration：
Measure-the way of distillation for being measured as GB/T8929 crude oil water contents of water content
The dehydration rate of crude oil is calculated as follows：
The dehydration rate %=(quality of the water contained in the water quality/crude oil deviate from from crude oil) * 100% of crude oil
Gas hydrocarbon content in crude oil is calculated as follows：
The gas hydrocarbon content %=(carburet hydrogen quality/crude oil feeding quality) * 100% of crude oil
The carburet hydrogen of the crude oil predominantly emergent gas caused by heating in crude oil dehydration, it is impossible to mixed with crude oil
It is integrated, and crude oil evaluation is also required to determine crude oil gas hydrocarbon content.
(4) after crude oil dehydration, the cleaning method of above-mentioned crude oil continuous dehydration device.
Need to clean it after the above-mentioned crude oil continuous still dehydration device of application carries out crude distillation dewater treatment, clearly
The method washed is：Added using including but not limited to No. 120 solvent naphthas, the petroleum ether that boiling point is 90 DEG C to 120 DEG C, toluene equal solvent
The mixed liquor of absolute ethyl alcohol is cleaned.About 100 DEG C of the temperature of secondary heater 22 and primary heater 12 is set, makes cleaning molten
The quantity that agent has about 50% enters the top of gas-liquid separation post, and 50% quantity enters gas-liquid separation column bottom, works as gas-liquid separation
Capital and bottom outflow solution are limpid, clean up stopping cleaning.The vent valves 313 of the bottom of feeding line 311 are opened, are released
Remaining cleaning solvent, and it is passed through nitrogen drying instrument.
Embodiment 1
Power-on, the condensation point and viscosity of based on crude set the temperature of the heater 32 of controllable temperature feed pump 33 and the 3rd as
50 DEG C, kept for 10 minutes.The temperature of secondary heater 22 and upper heater 121 is set as 200 DEG C, the temperature of lower heater 122
For 250 DEG C.The temperature of the second cooling component 51, light oil and water storage tank 52 is set as 1 DEG C, the temperature of the cooling component 41 of setting first
60℃.The chilling temperature of carburet hydrogen recycling can 53 is -90 DEG C.
The mass % of water content 53.1 crude oil is entered by controllable temperature feed pump (gear pump) flow velocity 16ml/min inlet amount
Row dehydration, it is 5 minutes that light oil and heavy oil, which distillate the time, and dewatering time is 230 minutes.3099 grams of crude oil feeding quality, abjection
1639 grams of water quality, dewatered oil water content is 0.1 mass %, and calculating obtains crude oil dehydration rate for 99.8 mass %, do not received
Collect gas.
Embodiment 2
The temperature of the heater 32 of controllable temperature feed pump 33 and the 3rd is set as 100 DEG C, is kept for 10 minutes.Setting second is heated
The temperature of device 22 and upper heater 121 is 300 DEG C, and the temperature of lower heater 122 is 300 DEG C.Setting second cools component 51, light
The temperature of oil and water storage tank 52 is 10 DEG C, 100 DEG C of the temperature of the cooling component 41 of setting first.The cooling temperature of carburet hydrogen recycling can 53
Spend for -100 DEG C.
The mass % of water content 1.1 crude oil is carried out by controllable temperature feed pump (gear pump) flow velocity 16ml/min inlet amount
Dehydration, it is 5 minutes that light oil and heavy oil, which distillate the time, and dewatering time is 230 minutes, and 3204 grams of crude oil feeding quality, crude oil takes off
35 grams of effluent characteristics, dewatered oil water content be vestige (<0.03 mass %), calculating obtains crude oil dehydration rate close to 100%, gas
5 grams of body hydrocarbonaceous amount, gas hydrocarbon content is 0.15 mass %.
Embodiment 3
The temperature of the heater 32 of controllable temperature feed pump 33 and the 3rd is set as 20 DEG C, is kept for 10 minutes.Setting second is heated
The temperature of device 22 and upper heater 121 is 200 DEG C, and the temperature of lower heater 122 is 250 DEG C.Setting second cools component 51, light
The temperature of oil and water storage tank 52 is 1 DEG C, the temperature 60 C of the cooling component 41 of setting first.The chilling temperature of carburet hydrogen recycling can 53
For -90 DEG C.
The mass % of water content 63.6 crude oil is entered by controllable temperature feed pump (gear pump) flow velocity 16ml/min inlet amount
Row dehydration, it is 5 minutes that light oil and heavy oil, which distillate the time, and dewatering time is 390 minutes, 5311 grams of crude oil feeding quality, abjection
3314 grams of water quality, dewatered oil water content is 3.2 mass %, and calculating obtains crude oil dehydration rate for 98.1 mass %.Do not receive
To gas.
Because dewatered oil water content is 3.2 mass %, standardization is not inconsistent, be that this carries out second dehydration to dewatered oil.
Second dehydration technological parameter is as follows：
The temperature of the heater 32 of controllable temperature feed pump 33 and the 3rd is set as 50 DEG C, is kept for 10 minutes.Setting second is heated
The temperature of device 22 is 200 DEG C, and the temperature of upper heater 121 is 210 DEG C, and the temperature of lower heater 122 is 260 DEG C.Setting second is dropped
Warm component 51, the temperature of distillation water storage tank 52 are 1 DEG C, the temperature 60 C of the cooling component 41 of setting first, carburet hydrogen recycling can 53
Chilling temperature be -90 DEG C.
Above-mentioned dehydration by controllable temperature feed pump (gear pump) flow velocity 16ml/min inlet amount to the mass % of water content 3.2
Crude oil is dehydrated again, and it is 5 minutes that light oil and heavy oil, which distillate the time, and dewatering time is 140 minutes, crude oil feeding quality
1810 grams, crude oil abjection 58 grams of water quality, second dehydration water content in crude oil be vestige (<0.03 mass %), calculating obtains crude oil
Dehydration rate is close to 100%.Do not receive gas.
Comparative example 1
Using laboratory conventional method, distilled using distillation still.Raw material dosage is same as Example 1, vapo(u)rizing temperature
For 250 DEG C, distillation time is 5 hours, and crude oil heated time is also 5 hours.
Test result：3099 grams of crude oil feeding quality, crude oil 1630 grams of water quality of abjection, is contained by the crude waters of GB/T 8929
Measure determination method and determine crude oil water content 53.1%, dewatered oil water content is 1.0 mass %, and calculating obtains crude oil dehydration rate and is
99.0 quality %.
Taken off it can be seen from test result in above-described embodiment 1 to 3 and comparative example 1 using crude oil continuous still of the present invention
Water installations carry out distillation dehydration to crude oil, and dehydration rate is apparently higher than common method of the prior art.And it is provided by the present invention
Device can continuous feed dehydration, light, heavy oil discharging time can be adjusted in feedstock amount, still-process as needed very
It is short, only 5-7 minutes, the decomposition that heavy oil is caused in dehydration due to heated can be prevented effectively from, gained crude oil after dehydration
Thermal change does not occur substantially for properties of samples.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing, still, the present invention is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the present invention, a variety of letters can be carried out to technical scheme
Monotropic type, these simple variants belong to protection scope of the present invention.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, can be combined by any suitable means, in order to avoid unnecessary repetition, the present invention to it is various can
The combination of energy no longer separately illustrates.
In addition, various embodiments of the present invention can be combined randomly, as long as it is without prejudice to originally
The thought of invention, it should equally be considered as content disclosed in this invention.
Claims (17)
1. a kind of crude oil continuous still dewatering, it is characterised in that this method includes wet crude being continuously passed through crude oil
It is provided with the feed duct line (31) of continuous still dehydration device charging conveying assembly (30), the charging conveying assembly (30)
Controllable temperature feed pump (33), the pre-add hot pipeline (21) entered back into preheating component (20) is preheated, and makes wet crude
In light oil and water, distilled subsequently into the housing in housing unit (11), the water and light oil in crude oil are from housing
Upper gaseous phase outlet discharge, enters light oil and water storage tank (52), water therein is from light after reclaiming component (50) condensation through distillation gas
Oil and the discharge of water storage tank (52) bottom, carburet hydrogen are discharged into carburet hydrogen recycling can (53) from light oil and water storage tank (52) top；
Heavy oil in crude oil is discharged from lower housing portion liquid-phase outlet, enters heavy oil recycling can after reclaiming component (40) condensation through heavy oil
(42)。
2. according to the method described in claim 1, wherein, described charging conveying assembly (30) includes：
The feed duct line (31), its end is connected with the pre-add hot pipeline (21) in preheating component (20)；
3rd heater (32), the temperature internal for adjusting the feed duct line (31).
3. method according to claim 2, wherein, the 3rd heater (32) is to be wrapped in the feed duct line
(31) the 3rd heating mantle of periphery.
4. according to the method described in claim 1, wherein, the feed duct line (31) includes：
Feeding line (311), which is provided with positioned at the feed(raw material)inlet on top, tapping valve (313) and leakage fluid dram positioned at bottom
, and superposed controllable temperature feed pump (33) (314)；
Feed-line (312), one end is connected on the feeding line (311), and positioned at the controllable temperature feed pump (33) and
Between the tapping valve (313), the other end is connected on the pre-add hot pipeline (21),
The wet crude is from the feeding line (311) continuously into the crude oil continuous still dehydration device.
5. method according to claim 2, wherein, wet crude is continuously passed through to crude oil continuous still dehydration device
During, the temperature for controlling the 3rd heater is 20~100 DEG C.
6. in accordance with the method for claim 1, wherein, it is described preheating component (20) include：
The pre-add hot pipeline (21), the arrival end for being located at middle part with the housing is connected,
Secondary heater (22), the temperature internal for adjusting the pre-add hot pipeline (21).
7. in accordance with the method for claim 6, wherein, preferably described secondary heater (22) is is wrapped in the pre-add heat pipe
Second heating mantle of line (21) periphery.
8. method according to claim 6, wherein, wet crude is continuously passed through to crude oil continuous still dehydration device
During, the temperature for controlling secondary heater is 100~300 DEG C.
9. according to the method described in claim 1, wherein, the housing unit (11) includes：
The housing, its middle part is provided with arrival end, and top sets the gaseous phase outlet, and bottom sets liquid-phase outlet；
Upper cover (113), the open top with the housing is tightly connected；
Low head (114), is tightly connected with the bottom opening of the housing；
The housing unit (11) is provided with primary heater (12), and the primary heater (12) is used to adjust in the housing
The temperature in portion.
10. method according to claim 9, wherein, the primary heater (12) is to be wrapped in the housing periphery
First heating mantle.
11. according to the method described in claim 1, wherein, the pre-add hot pipeline (21) is to deviate 5 °~30 ° directions of horizontal plane
Extend downwardly and be connected with the housing inlet port end.
12. according to the method described in claim 1, wherein, the distillation gas, which reclaims component (50), to be included：
Second cooling component (51), one end is connected with the gaseous phase outlet of the housing unit (11) housing；
Light oil and water storage tank (52), are connected with the other end of the described second cooling component (51), and the light oil and water storage tank
(52) it is provided with gaseous phase outlet；
Carburet hydrogen recycling can (53), is connected with the gaseous phase outlet of the light oil and water storage tank (52).
13. method according to claim 12, wherein, heavy oil, which reclaims component (40), to be included：
First cooling component (41), one end is connected with the liquid-phase outlet of the housing unit (11) housing；
Heavy oil recycling can (42), is connected with the other end of the described first cooling component (41).
14. the method according to claim 12 or 13, wherein, the first cooling component (41) or the second cooling group
Part (51) includes：
Inner tube (411), one end is connected with the liquid-phase outlet of the housing unit (11) housing, the other end and the heavy oil recycling can
(42) it is connected；
Outer tube (412), is wrapped in the periphery of said inner tube (411), is formed between the outer tube (412) and said inner tube (411)
Temperature-reducing medium flowing lumen (413).
15. the method according to claim 12 or 13, wherein, the bottom of the heavy oil recycling can (42) is provided with draining valve
And oil discharge outlet (422) (421)；The bottom of the light oil and water storage tank (52) is provided with draining valve (521) and discharge outlet (522)；Institute
The top for stating carburet hydrogen recycling can (53) is provided with air bleeding valve (532) and exhaust outlet (533).
16. method according to claim 12, wherein, component (50) condensation is reclaimed from housing upper gas phase using distillation gas
When exporting the water and light oil in the crude oil of discharge, the temperature for controlling the second cooling component (51) and light oil and water storage tank (52) is
1~15 DEG C, the temperature of carburet hydrogen recycling can (53) is -80~-100 DEG C.
17. method according to claim 13, wherein, component (40) condensation is reclaimed using heavy oil and gone out from lower housing portion liquid phase
Mouthful discharge crude oil in heavy oil when, control first cooling component (41) and heavy oil recycling can (42) temperature be 20~100 DEG C.
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| CN201410584023.1A CN105623706B (en) | 2014-10-27 | 2014-10-27 | Crude oil continuous still dewatering |
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| DE2153162A1 (en) * | 1971-10-26 | 1973-05-03 | Metallgesellschaft Ag | Water extraction from gas oil - by steam treatment and expansion in flash zone of stripper |
| CN1935961A (en) * | 2006-09-14 | 2007-03-28 | 上海交通大学 | Hardening oil on-line dehydration apparatus |
| CN1986061A (en) * | 2005-12-19 | 2007-06-27 | 中国石油化工股份有限公司 | Distillation dewatering set and its dewatering process using it |
| CN2923705Y (en) * | 2006-05-12 | 2007-07-18 | 海安华安石油科研仪器有限公司 | Crude-oil efficient dewatering apparatus |
| CN202554970U (en) * | 2012-04-13 | 2012-11-28 | 重庆九潮环保设备有限公司 | Oil liquid vacuum flash device |
| CN202912907U (en) * | 2012-10-24 | 2013-05-01 | 中国石油化工股份有限公司 | Device for dehydrating oils with distillation method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2153162A1 (en) * | 1971-10-26 | 1973-05-03 | Metallgesellschaft Ag | Water extraction from gas oil - by steam treatment and expansion in flash zone of stripper |
| CN1986061A (en) * | 2005-12-19 | 2007-06-27 | 中国石油化工股份有限公司 | Distillation dewatering set and its dewatering process using it |
| CN2923705Y (en) * | 2006-05-12 | 2007-07-18 | 海安华安石油科研仪器有限公司 | Crude-oil efficient dewatering apparatus |
| CN1935961A (en) * | 2006-09-14 | 2007-03-28 | 上海交通大学 | Hardening oil on-line dehydration apparatus |
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| CN105623706A (en) | 2016-06-01 |
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