CN105623706A - Crude oil continuous distillation and dehydration method - Google Patents
Crude oil continuous distillation and dehydration method Download PDFInfo
- Publication number
- CN105623706A CN105623706A CN201410584023.1A CN201410584023A CN105623706A CN 105623706 A CN105623706 A CN 105623706A CN 201410584023 A CN201410584023 A CN 201410584023A CN 105623706 A CN105623706 A CN 105623706A
- Authority
- CN
- China
- Prior art keywords
- oil
- assembly
- crude oil
- temperature
- housing
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
The invention discloses a crude oil continuous distillation and dehydration method. The dehydration method includes that water-containing crude oil is continuously introduced into a feeding and conveying pipeline of a feeding and conveying assembly of an crude oil continuous distillation and dehydration device, then enters a pre-heating pipeline in a pre-heating assembly, is pre-heated, next enters a shell body of a shell body assembly and is distilled; water and light oil in the crude oil are discharged from a gas phase outlet at the upper part of the shell body, are condensed by a distillation gas recovery assembly and then enter a light oil and water storage tank, wherein the water is discharged from the bottom of the light oil and water storage tank, and gas hydrocarbons are discharged from the upper part of the light oil and water storage tank and then enter a gas hydrocarbon recovery tank; heavy oil in the crude oil is discharged from a liquid phase outlet at the lower part of the shell body, is condensed by a heavy oil recovery assembly and then enters a heavy oil recovery tank. A to-be-dehydrated material (such as the crude oil) is subjected to pre-heating treatment on the pre-heating pipeline, and then the to-be-dehydrated material after heating treatment is distilled in the shell body assembly and is subjected to gas-liquid separation at the same time to achieve 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, in sample, the analysis detection project of sample can be had a direct impact by the existence of water, such as density, flash-point, boiling range, viscosity, ash, carbon residue, condensation point, metal etc., therefore moisture crude oil and oil product must carry out dehydration before being evaluated, analyzing detection.
At present, have multiple at use for laboratory in the method for the dehydration of crude oil, including deposition dehydrating method, autoclave evaporation, EDN, microwave dehydration method and distillation dehydration method etc. Wherein distillation dehydration method is by making water vapor steam oil product heating, reaching the purpose of oil dehydrating. Water in oil product almost can all be taken off by the method, and do not need to add the external agent such as demulsifier, comparing with other dewatering, have that dehydration is more complete, simple and easy to do, do not affect the features such as oil product component, applying so being highly suitable in crude oil evaluation, analysis of oil laboratory.
The distillation dehydration method that current laboratory is common, it is common that in a fixing distillating still, raw material is distilled, and then make the moisture evaporation in crude oil, to realize the purpose of the dehydration of crude oil. It is crude oil is joined in fixing distillating still, by adding thermal still, so that moisture evaporation and then dehydration, common device includes: such as gives a kind of crude oil dewatering instrument in Chinese patent CN202606174U, gives a kind of way of distillation oil dehydrating plant etc. in Chinese patent CN202912907U.
Existing this distillation dehydration method, on the one hand owing to being subject to the limitation of device volume, the amount of the dewatered oil every time obtained is limited, if needing to obtain larger amount of dewatered oil, then needs repetitive operation repeatedly, not only consumes energy but also consuming time. On the other hand owing to being arranged in the crude oil of distillating still, along with the volatilization of moisture, water content gradually decreases, the crude oil reduced for moisture is then more and more higher to the requirement of vapo(u)rizing temperature, in order to obtain the satisfactory crude oil of dehydration rate, then need to extend dewatering time, increase dehydration temperaturre.
Summary of the invention
It is an object of the invention to provide a kind of crude oil continuous still dewatering, crude oil can be carried out continuous fast dewatering, crude charging capacity is big, and dehydration temperaturre is low, and can control continuous feed flow velocity.
The invention provides a kind of crude oil continuous still dewatering, the method includes the feed duct line that wet crude passes into crude oil continuous still dehydration device charging conveying assembly continuously, enter back into the pipeline that preheats preheating in assembly to preheat, distill subsequently into the housing in housing unit, water and light oil in crude oil are discharged from housing upper gaseous phase outlet, reclaim through distillation gas and enter light oil and water storage tank after assembly condensation, water therein is discharged bottom light oil and water storage tank, 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, reclaims through heavy oil and enters heavy oil recycling can after assembly condensation.
Above-mentioned crude oil continuous still dewatering, pipeline is treated dehydrated material (such as crude oil) carry out preheating process preheating, then the material to be drained off through heat treated is carried out in housing unit distillation vapor-liquid separation simultaneously to realize dehydration. This method has good operability, inlet amount can be adjusted as required, continuous feed is to obtain dewatered oil, continuous feed and discharging are conducive to shortening the material time of staying in distillation dehydration device, avoiding crude oil decomposes in dehydration, after making dehydration, crude oil remains in that original character is constant.
Simultaneously, above-mentioned crude oil continuous still dewatering owing to preheating material in preheating pipeline, preheating process makes the light component in material and water, so that material enters to distill rapidly when space becomes big in housing unit carries out gas-liquid separation, advantageously reduce vapo(u)rizing temperature, energy consumption, and deviate from the moisture in crude oil better.
Other features and advantages of the present invention will be described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and constitutes the part of description, is used for explaining the present invention, but is not intended that limitation of the present invention together with detailed description below.
Fig. 1 is the structural representation of the crude oil continuous still dehydration device used of the inventive method.
Description of reference numerals
11 housing unit 111 housing upper
112 lower housing portion 113 upper covers
114 low heads
12 primary heater 121 upper heaters
122 times heaters
20 preheat assembly 21 preheats pipeline
22 secondary heater 23 plug at end part heads
30 charging conveying assembly 31 feed-lines
311 feeding line 312 feed-lines
313 tapping valve 314 leakage fluid drams
32 the 3rd heater 33 controllable temperature feed pumps
40 heavy oil reclaim assembly 41 first cooling assembly
Pipe 412 outer tube in 411
413 temperature-reducing medium flowing lumen 42 heavy oil recycling cans
421 draining valve 422 oil drain outs
50 distillation gas reclaim assembly 51 second cooling assembly
52 light oil and water storage tank 521 drain valve
522 discharge outlet 53 carburet hydrogen recycling cans
531 intake valve 532 air bleeding valves
533 air vents
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail. It should be appreciated that detailed description of the invention described herein is merely to illustrate and explains the present invention, it is not limited to the present invention.
In the present invention, term " heavy oil " and term " light oil " are relative concept. Wherein " heavy oil " refers in distillation dehydration process, the boiling point fraction more than 300 DEG C, and " light oil " refers to the fraction being not more than 300 DEG C at distillation dehydration process mid-boiling point, and carburet hydrogen is C3��C4 hydrocarbon. If containing carburet hydrogen in crude oil, then being carried by light oil and discharge from the top of housing unit middle shell.
Inventor proposes a kind of crude oil continuous still dewatering. As shown in Figure 1, the method includes the feed duct line 31 that wet crude passes into crude oil continuous still dehydration device charging conveying assembly 30 continuously, enter back into the pipeline 21 that preheats preheating in assembly 20 to preheat, distill subsequently into the housing in housing unit 11, water and light oil in crude oil are discharged from housing upper gaseous phase outlet, reclaim through distillation gas and enter light oil and water storage tank 52 after assembly 50 condensation, water therein is discharged bottom light oil and water storage tank 52, and carburet hydrogen is 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, reclaims through heavy oil and enters heavy oil recycling can 42 after assembly 40 condensation.
Above-mentioned crude oil continuous still dewatering, by treating dehydrated material (such as crude oil) on pipeline and carry out preheating process preheating, while then carrying out distilling in housing unit by the material to be drained off through heat treated, vapor-liquid separation is to realize dehydration. This method has good operability, inlet amount can be adjusted as required, continuous feed is to obtain dewatered oil, continuous feed and discharging are conducive to the time of staying shortening material in the de-device of distillation, avoiding crude oil decomposes in dehydration, after making dehydration, crude oil keeps original character constant as far as possible.
Simultaneously, above-mentioned crude oil continuous still dewatering, owing to material being preheated in preheating pipeline, preheating process makes the light component in material and water, so that material enters to distill rapidly when space becomes big in housing unit carries out gas-liquid separation, advantageously reduce vapo(u)rizing temperature, energy consumption, and deviate from the moisture in crude oil quickly.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, charging conveying assembly 30 includes: feed duct line 31 and the 3rd heater 32. The end of feed duct line 31 is connected with the pipeline 21 that preheats preheated in assembly 20; 3rd heater 32 is for adjusting the temperature within described feed duct line 31.
In practical operation, in charging conveying assembly 30, temperature should lower than the temperature preheated in assembly 20, treat dehydrated material tentatively heat owing to being provided with charging conveying assembly 30 before heating assembly 20, the temperature making material to be drained off promotes, it is easy to inflow preheats assembly 20 and is heated. When now material inflow heating assembly 20 is heated, the temperature difference of required intensification is relatively small, it is possible to shorten the length of conveying pipeline in heating assembly 20, to reduce the energy loss that longer conveying pipeline brings.
In the preferred embodiment of the present invention, wet crude is passed into continuously in the process of crude oil continuous still dehydration device, control above-mentioned 3rd heater 32 with by heating crude oil to 20��100 DEG C, to promote crude oil to be tentatively heated. Preferably, above-mentioned 3rd heater 32 can be multiple heating members being distributed on feed duct line 31, it is more preferred to, the 3rd heater 32 is the Acanthopanan trifoliatus (L.) Merr. hot jacket being wrapped in feeding line 31 periphery.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, also including controllable temperature feed pump 33 in charging conveying assembly 30, controllable temperature feed pump 33 is arranged on feed duct line 31. This controllable temperature feed pump 33 may advantageously facilitate that to be similar to crude oil this readily flowed after being heated for the material to be drained off of dope under normal temperature, and then the continuous feed amount of controllable material to be drained off. For crude oil, the condensation point of based on crude and viscosity temperature, controllable temperature feed pump temperature control scope 20��100 DEG C can be determined in practical operation.
Preferably, in the crude oil continuous still dehydration device that the above-mentioned crude oil continuous still dewatering of the present invention uses, feed duct line 31 includes feeding line 311 and feed-line 312. Wet crude from feeding line 311 continuously into described crude oil continuous still dehydration device. Wherein, feeding line 311 is provided with the feed(raw material)inlet on top, is positioned at tapping valve 313 and the leakage fluid dram 314 of bottom and superposed controllable temperature feed pump 33; Feed-line 312 one end is connected on feeding line 311, and between controllable temperature feed pump 33 and tapping valve 313, the other end is connected to and preheats on pipeline 21.
Adopt the crude oil continuous still dehydration device with this structure, feed duct line 31 is divided into feeding line 311 and feed-line 312, be conducive to the charging of material to be drained off on the one hand, particularly with the charging of the material to be drained off of thick existence, on the other hand, being easy to the cleaning after the distillation dehydration end of job, opening by will be located in the tapping valve 313 of feeding line 311 bottom, cleanout fluid can be made simultaneously to be discharged by feeding line 311 and feed-line 312. Meanwhile, tapping valve 313 is set in feeding line 311 bottom, it is also possible to for after by solvent clean continuous still dehydrator, residual solvent in blow-down pipe, pass into nitrogen and purge instrument.
Preferably, the draw ratio of above-mentioned feed duct line 31 is 10��300. The draw ratio of feed duct line 31 is not limited to above-mentioned scope in the present invention, is disposed in above-mentioned scope and has so that material to be drained off heating is more uniformly distributed, and the effect that dehydrating effect is more preferably.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, preheat assembly 20 and include: preheat pipeline 21 and secondary heater 22. Preheat pipeline 21 be positioned at housing middle part arrival end be connected. Secondary heater 22 is for adjusting the temperature preheated within pipeline 21. Above-mentioned in the crude oil continuous still dehydration device that the above-mentioned crude oil continuous still dewatering of the present invention uses, for secondary heater 22 not particular/special requirement, as long as being capable of adjusting the requirement of temperature, for instance secondary heater 22 can be multiple heating members being distributed in and preheating on pipeline 21. Secondary heater 22 is be wrapped in and preheat pipeline 21 periphery second add hot jacket in the preferred embodiment of the present invention. Add the periphery being wrapped in material to be heated that hot jacket can be more complete so that heating-up temperature is more uniformly distributed.
Preferably, in above-mentioned crude oil continuous still dewatering, being passed into by wet crude in the process of crude oil continuous still dehydration device continuously, the temperature controlling secondary heater is 100��300 DEG C. The temperature of secondary heater is not limited to above-mentioned scope in the present invention, it is above-mentioned scope by its limit temperature, be conducive to pipeline 21 making light component in material (wet crude) and water preheating, so that material enters to distill rapidly when space becomes big in housing unit carries out gas-liquid separation, advantageously reduce vapo(u)rizing temperature, energy consumption, and deviate from the moisture in crude oil better.
Preferably, in the crude oil continuous still dehydration device that the above-mentioned crude oil continuous still dewatering of the present invention uses, preheating pipeline 21 draw ratio is 2��30, more preferably 10��20. The draw ratio preheating pipeline 21 in the present invention is not limited to above-mentioned scope, is disposed in above-mentioned scope and has so that material to be drained off is more susceptible to thermal evaporation, to improve dewatering efficiency.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, housing unit 11 includes: housing, upper cover 113 and low head 114. Housing central section is provided with arrival end, and top sets gaseous phase outlet, bottom sets liquid-phase outlet; The open top of upper cover 113 and housing is tightly connected; The bottom opening of low head 114 and housing is tightly connected. Wherein preferably gaseous phase outlet is arranged near upper cover 113, it is preferable that liquid-phase outlet is arranged near low head 114, and arrival end is between gaseous phase outlet and liquid-phase outlet. This housing unit 11 arranges upper cover 113 and low head 114 also helps its disassembly, cleaning and replacing, and then is conducive to extending the service life of housing unit 11.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, housing unit 11 is provided with primary heater 12, and primary heater 12 is for adjusting the temperature of described enclosure interior.
In the present invention for primary heater 12 not particular/special requirement, as long as being capable of adjusting the requirement of temperature, such as primary heater 12 can be the heating coil being arranged on enclosure interior, primary heater 12 is be wrapped in the first of housing unit 11 middle shell periphery to add hot jacket in the preferred embodiment of the present invention, adds the periphery being wrapped in material to be heated that hot jacket can be more complete so that heating-up temperature is more uniformly distributed.
Above-mentioned housing is preferably gas-liquid separation post, when the material to be drained off of heated process enters the housing of housing unit 11, begins to carry out vapor-liquid separation, and gas is to gaseous phase outlet flowing above, and liquid flows to the liquid-phase outlet being positioned below. It is adjusted by arranging the primary heater 12 temperature to enclosure interior, is conducive to promoting the material being in flow regime to distill further, and then improve dehydration rate.
Preferably, in the crude oil continuous still dehydration device that the above-mentioned crude oil continuous still dewatering of the present invention uses, preheat material pipeline 21 and be preferably connected with the middle part of housing unit 11 middle shell, housing unit 11 is divided into housing upper 111 and lower housing portion 112. Now, primary heater 12 includes upper heater 121 and lower heater 122. Upper heater 121 is for adjusting the internal temperature of housing upper 111; Lower heater 122 is for adjusting the internal temperature of lower housing portion 112.
In practical operation, can so that upper heater 121 be identical with secondary heater 22 temperature (such as when crude oil is carried out dehydration, the temperature of upper heater 121 and secondary heater 22 is 100��300 DEG C), preferably make the temperature temperature (such as when crude oil is carried out dehydration, the temperature of lower heater 122 is higher than the temperature of upper heater 121 10��50 DEG C) higher than upper heater of lower heater 122. By adjusting the temperature of upper heater and lower heater, the liquid flowing downwardly into lower housing portion 112 can be promoted to carry out distillation dehydration further on the one hand, on the other hand in view of the temperature difference between housing upper 111 and lower housing portion 112, light hydrocarbon and water can be promoted to be easier to flow up, and then promote the carrying out of dehydration by evaporation.
Preferably, the ratio of height to diameter of above-mentioned housing unit 11 middle shell inner chamber is 5��60, it is preferred to 10��30. In practical operation, it is possible to according to the quantity heating assembly in above-mentioned continuous still dehydrator, adjust the ratio of height to diameter of housing unit 11 middle shell inner chamber, to promote material to be drained off heating to be more uniformly distributed, dehydrating effect is more preferably.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, preheat pipeline 21 and extend downwardly and be connected with described housing inlet port end deviateing horizontal plane 5 �㡫30 ��. Adopt this downward-sloping pipeline, be conducive to the material to be drained off after promoting heated process to flow in housing. It is further preferable that preheat pipeline 21 away from one end of housing there is cleaning opening, and with clean the plug at end part head 23 that opening is tightly connected.
Preferably, the above-mentioned internal diameter internal diameter more than feed duct line 31 preheating pipeline 21, more preferably preheat 2��10 times of the internal diameter that internal diameter is feed duct line 31 of pipeline 21. This structure is conducive to adapting to the pressure change of heat treated material to be drained off on the one hand, improves processing safety, and the material to be drained off after being conducive to heated process on the other hand is quickly flowed in the housing in housing unit 11 smoothly.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, preheat assembly 20 and can be many groups, charging conveying assembly 30 is and preheats assembly 20 many groups one to one, it is preferably 2-5 group, for instance 2 groups, 3 groups, 4 groups or 5 groups. The many groups of settings preheating assembly 20 and many group charging conveying assemblies 30 are more suitable for the industrialized production requirement to equipment. In practical operation, it is possible to preheat assembly 20 by each group as required and be circumferentially connected with the housing in housing unit 11 respectively, or it is connected with the housing in described housing unit 11 at differing heights respectively. For each group being preheated the device that assembly 20 is circumferentially connected respectively with the housing in housing unit 11, it is possible to for many group materials are run simultaneously, improve timeliness. For preheating, by each group, the device that assembly 20 is connected with the housing in housing unit 11 respectively at differing heights, it is possible to the difference according to material water ratio, select the inflow being more suitable for, it is also possible to materials different for moisture content is carried out simultaneously distillation dehydration process.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, distillation gas reclaims assembly 50 and includes: the second cooling assembly and 51, light oil and water storage tank 52 and carburet hydrogen recycling can 53. Second cooling assembly 51 one end is connected with the gaseous phase outlet of housing unit 11 housing; Light oil is connected with second other end lowering the temperature assembly 51 with water storage tank 52, and light oil and water storage tank 52 are provided with gaseous phase outlet; Carburet hydrogen recycling can 53 is connected with the gaseous phase outlet of light oil and water storage tank 52.
By adopting this distillation gas to reclaim assembly 50, by light oil and Water Sproading and separate. Lowered the temperature through the second admixture of gas lowering the temperature assembly 51, it is delivered to light oil and water storage tank 52 (preferably the periphery of this distilled water storage tank 52 is formed with vacuum interlayer), being separated with water by the light oil being in a liquid state in light oil and water storage tank 52, carburet hydrogen is delivered in carburet hydrogen recycling can 53 and separates with light oil again.
Preferably, in the above-mentioned crude oil continuous still dewatering of the present invention, when adopting distillation gas recovery assembly 50 to condense the water from the crude oil that housing upper gaseous phase outlet is discharged and light oil, the temperature controlling the second cooling assembly 51 and light oil and water storage tank 52 is 1 DEG C��15 DEG C, and the temperature of carburet hydrogen recycling can 53 is-80��-100 DEG C.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, heavy oil reclaims assembly and includes the first cooling assembly 41 and heavy oil recycling can 42. First cooling assembly 41 one end is connected with the liquid-phase outlet of the housing in housing unit 11; Heavy oil recycling can 42 is connected with first other end lowering the temperature assembly 41. It is simple that this heavy oil reclaims modular construction, and operability is stronger. In practical operation, it is cooled through the first heavy oil lowering the temperature assembly 41 and heavy oil recycling can 42 can be adopted to reclaim.
Preferably, in the above-mentioned crude oil continuous still dewatering of the present invention, when adopting heavy oil to reclaim the heavy oil that assembly 40 condenses from the crude oil that lower housing portion liquid-phase outlet is discharged, the temperature controlling the first cooling assembly 41 and heavy oil recycling can 42 is 20��100 DEG C.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, the first cooling assembly 41 and the second cooling assembly 51 structure specifically do not limit, as long as can carry out lowering the temperature. In the preferred embodiment of the present invention, above-mentioned first cooling assembly 41 is identical with the second cooling assembly 51 structure, and for the first cooling assembly 41, this first cooling assembly 41 includes interior pipe 411 and outer tube 412. Interior pipe 411 one end is connected with the liquid-phase outlet of the housing in described housing unit 11, and the other end is connected with heavy oil recycling can 42; Outer tube 412 is wrapped in the periphery of interior pipe 411, forms temperature-reducing medium flowing lumen 413 between outer tube 412 and interior pipe 411.
This cooling modular construction, not only simple in construction, it is easy to make, and its cooling-down effect is comparatively uniform. When being applied to laboratory equlpment, it can adopt glass material to make so that observing. Preferably wherein interior pipe 411 is with respect to the horizontal plane downward-sloping along Flow of Goods and Materials direction, and this downward-sloping structure is conducive to liquid in interior pipe 411 to discharge. In practical operation, temperature-reducing medium being passed into temperature-reducing medium flowing lumen 413, this temperature-reducing medium preferably cools down water.
In the preferred embodiment of the present invention, in the crude oil continuous still dehydration device that above-mentioned crude oil continuous still dewatering uses, the bottom of heavy oil recycling can is provided with draining valve 421 and oil drain out 422, so that the discharge of heavy oil, the bottom of light oil and water storage tank is provided with drain valve 521 and discharge outlet 522, in order to the discharge of distilled water; The top of carburet hydrogen recycling can is provided with air bleeding valve 532 and air vent 533, in order to fixed gas in device, the discharge of nitrogen used during as cleaned.
Beneficial effects of the present invention is further illustrated below with reference to specific embodiment.
(1) equipment that below embodiment adopts is as it is shown in figure 1, concrete structure is as follows:
In crude oil continuous still dehydration device, continuous still dehydrator includes: housing unit 11, primary heater 12, preheat assembly 20, charging conveying assembly 30. Wherein housing unit 11 includes upper cover 113 that the open top of gas-liquid separation post (ratio of height to diameter of gas-liquid separation post enclosure interior is 20) and gas-liquid separation post is tightly connected and the low head 114 that the bottom opening with gas-liquid separation post is tightly connected. Primary heater (first adds hot jacket) 12 is wrapped in gas-liquid separation post periphery. Preheat assembly 20 to include preheating pipeline 21 (draw ratio is 10) and being wrapped in the secondary heater (second adds hot jacket) 22 preheating pipeline 21 periphery. Preheat pipeline 21 to deviate horizontal plane 10 �� and extend the middle part with gas-liquid separator 10 downwardly and be connected and be classified as housing upper 111 and lower housing portion 112. Primary heater (first adds hot jacket) 12 includes the upper heater 121 for adjusting the temperature within housing upper 111 and for adjusting the lower heater 122 of the temperature within lower housing portion 112. Charging conveying assembly 30 is arranged on the upstream preheating assembly 20, including feed duct line 31 (feed duct line 31 draw ratio is 100, and the internal diameter ratio preheating pipeline 21 and feed duct line 31 is 5) and the 3rd heater (Acanthopanan trifoliatus (L.) Merr. hot jacket) 32 being wrapped in its periphery. Wherein feed duct line 31 includes feeding line 311 and is connected to feeding line 311 and the feed-line 312 preheated between 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, is provided with controllable temperature feed pump 33 between feed(raw material)inlet and tapping valve 313.
Crude oil continuous still dehydration device: include above-mentioned continuous still dehydrator, and the distillation gas recovery assembly 50 that the heavy oil being connected with the liquid-phase outlet of gas-liquid separation post in continuous still dehydrator reclaims assembly 40, gaseous phase outlet with gas-liquid separation post is connected. Heavy oil reclaims the first cooling assembly 41 that assembly 40 includes being connected and the heavy oil recycling can being connected with the first cooling assembly 41 with the liquid-phase outlet of gas-liquid separation post. First cooling assembly 41 includes the interior pipe that is connected between the liquid-phase outlet of gas-liquid separation post and heavy oil recycling can 42, and is wrapped in the outer tube 412 of the periphery of said inner tube 411, forms temperature-reducing medium flowing lumen 413 between outer tube 412 and interior pipe 411. The bottom of heavy oil recycling can is provided with draining valve 421 and oil drain out 422. Distillation gas reclaims the second cooling assembly 51, light oil and water storage tank 52 and the carburet hydrogen recycling can 53 that assembly 50 includes being sequentially connected with. Wherein the second cooling assembly 51 is identical with the first cooling assembly 41 structure, and the bottom of light oil and water storage tank 52 is provided with drain valve 521 and discharge outlet 522, and the top of carburet hydrogen recycling can is provided with air bleeding valve 532 and air vent 533.
(2) for crude oil, the using method of above-mentioned crude oil continuous still dehydration device is described.
Power-on, the condensation point of based on crude and viscosity set the temperature of controllable temperature feed pump 33 and the 3rd heater 32 as 1 DEG C to 80 DEG C, control crude oil flow velocity and are 0.5-2 l/h. Setting the temperature of secondary heater 22 and upper heater 121 as 120 DEG C to 260 DEG C, the temperature of lower heater 122 is 150 DEG C to 300 DEG C. Set the temperature of the second cooling assembly 51, light oil and water storage tank 52 as 1-15 DEG C, set the temperature 20 DEG C to 100 DEG C of the first cooling assembly 41. If crude oil is relatively light, containing gases such as carbon 3, carbon 4, the chilling temperature that need to control carburet hydrogen recycling can 53 in advance is-80 DEG C to-90 DEG C. After about 10 minutes, the temperature that instrument sets reaches setting value, starts controllable temperature feed pump 33, crude oil sequentially passes through charging conveying assembly, preheat assembly be heated after, flow in gas-liquid separation post. In gas-liquid separation post, water and light oil constituents and heavy oil component are distilled separation, after the water of gasification and oil gas rise to gaseous phase outlet on gas-liquid separation post and enter the second cooling assembly 51, it is cooled into liquid, flowing in light oil and water collecting tank 52, carburet hydrogen therein enters in the carburet hydrogen recycling can 53 of-80 DEG C to-90 DEG C. The heavy oil stream not gasified in gas-liquid separation post, to liquid-phase outlet at the bottom of gas-liquid separation post, flows in heavy oil recycling can 42 after the second cooling assembly 41. After the crude oil sample after continuous still dehydration reaches the amount of demand, stop dehydration. Release moisture from light oil and water storage tank 52 end, light oil in light oil and water storage tank 52 is mixed with heavy oil in heavy oil recycling can 42, as dewatered oil sample.
Crude oil sample after dehydration is pressed GB/T8929 detecting crude oil water content method and is measured water content, if water content requires (0.3 mass %) lower than the water content of crude oil evaluation, terminates the dehydration of crude oil. If water content requires (0.3 mass %) higher than the water content of crude oil evaluation, the dewatered oil of collection is reentered controllable temperature feed pump 33 and carries out distillation dehydration again, till water content requires (0.3%) lower than the water content of crude oil evaluation.
(3) water content of crude oil, the water content of crude oil after dehydration, the measurement of dehydration of crude oil rate, computational methods are as follows:
Mensuration-the way of distillation being measured as GB/T8929 crude oil water content 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
Carburet hydrogen content in crude oil is calculated as follows:
The carburet hydrogen content %=(carburet hydrogen quality/crude oil feeding quality) * 100% of crude oil
The carburet hydrogen of crude oil is mainly in dehydration of crude oil process because adding thermally-induced emergent gas, it is impossible to be mixed into one with crude oil, and crude oil evaluation is also required to measure crude oil carburet hydrogen content.
(4) after the dehydration of crude oil, the cleaning method of above-mentioned crude oil continuous dehydration device.
Needing it is carried out applying after above-mentioned crude oil continuous still dehydration device carries out crude distillation processed, the method for cleaning is: uses and includes but not limited to that petroleum ether that No. 120 solvent naphthas, boiling point are 90 DEG C to 120 DEG C, toluene equal solvent add the mixed liquor of dehydrated alcohol and be carried out. Set the temperature about 100 DEG C of secondary heater 22 and primary heater 12, cleaning solvent is made to have the quantity of about 50% to enter the top of gas-liquid separation post, the quantity of 50% enters gas-liquid separation column bottom, when gas-liquid separation capital and bottom outflow solution are limpid, clean up stopping and cleaning. Open the vent valves 313 of feeding line 311 bottom, release remaining cleaning solvent, and pass into nitrogen and dry up instrument.
Embodiment 1
Power-on, the condensation point of based on crude and viscosity set the temperature of controllable temperature feed pump 33 and the 3rd heater 32 as 50 DEG C, keep 10 minutes. Setting the temperature of secondary heater 22 and upper heater 121 as 200 DEG C, the temperature of lower heater 122 is 250 DEG C. Set the temperature of the second cooling assembly 51, light oil and water storage tank 52 as 1 DEG C, set the temperature 60 C of the first cooling assembly 41. The chilling temperature of carburet hydrogen recycling can 53 is-90 DEG C.
By the inlet amount of controllable temperature feed pump (gear pump) flow velocity 16ml/min, the crude oil of water content 53.1 mass % carrying out dehydration, light oil and heavy oil to distillate the time and be 5 minutes, dewatering time is 230 minutes. Crude oil feeding quality 3099 grams, deviates from water quality 1639 grams, and dewatered oil water content is 0.1 mass %, and it is 99.8 mass % that calculating obtains dehydration of crude oil rate, it does not have collect gas.
Embodiment 2
Set the temperature of controllable temperature feed pump 33 and the 3rd heater 32 as 100 DEG C, keep 10 minutes. Setting the temperature of secondary heater 22 and upper heater 121 as 300 DEG C, the temperature of lower heater 122 is 300 DEG C. Set the temperature of the second cooling assembly 51, light oil and water storage tank 52 as 10 DEG C, set the temperature 100 DEG C of the first cooling assembly 41. The chilling temperature of carburet hydrogen recycling can 53 is-100 DEG C.
By the inlet amount of controllable temperature feed pump (gear pump) flow velocity 16ml/min, the crude oil of water content 1.1 mass % is carried out dehydration, light oil and heavy oil distillate the time and are 5 minutes, dewatering time is 230 minutes, crude oil feeding quality 3204 grams, water quality 35 grams deviate from by crude oil, and dewatered oil water content is vestige (< 0.03 mass %), calculates and obtains dehydration of crude oil rate close to 100%, carburet hydrogen quality 5 grams, carburet hydrogen content is 0.15 mass %.
Embodiment 3
Set the temperature of controllable temperature feed pump 33 and the 3rd heater 32 as 20 DEG C, keep 10 minutes. Setting the temperature of secondary heater 22 and upper heater 121 as 200 DEG C, the temperature of lower heater 122 is 250 DEG C. Set the temperature of the second cooling assembly 51, light oil and water storage tank 52 as 1 DEG C, set the temperature 60 C of the first cooling assembly 41. The chilling temperature of carburet hydrogen recycling can 53 is-90 DEG C.
By the inlet amount of controllable temperature feed pump (gear pump) flow velocity 16ml/min, the crude oil of water content 63.6 mass % is carried out dehydration, light oil and heavy oil distillate the time and are 5 minutes, dewatering time is 390 minutes, crude oil feeding quality 5311 grams, deviate from water quality 3314 grams, dewatered oil water content is 3.2 mass %, and it is 98.1 mass % that calculating obtains dehydration of crude oil rate. Do not receive gas.
Owing to dewatered oil water content is 3.2 mass %, do not meet standard, for this, dewatered oil is carried out second dehydration. Second dehydration technological parameter is as follows:
Set the temperature of controllable temperature feed pump 33 and the 3rd heater 32 as 50 DEG C, keep 10 minutes. Setting secondary heater 22 temperature as 200 DEG C, the temperature of upper heater 121 is 210 DEG C, and the temperature of lower heater 122 is 260 DEG C. Set second cooling assembly 51, distilled water storage tank 52 temperature as 1 DEG C, set first cooling assembly 41 temperature 60 C, the chilling temperature of carburet hydrogen recycling can 53 is-90 DEG C.
By the inlet amount of controllable temperature feed pump (gear pump) flow velocity 16ml/min, the above-mentioned dewatered oil of water content 3.2 mass % is carried out dehydration again, light oil and heavy oil distillate the time and are 5 minutes, dewatering time is 140 minutes, crude oil feeding quality 1810 grams, water quality 58 grams deviate from by crude oil, second dehydration water content in crude oil is vestige (< 0.03 mass %), calculates and obtains dehydration of crude oil rate close to 100%. Do not receive gas.
Comparative example 1
Adopt laboratory conventional method, utilize distillating still to distill. Raw material dosage is identical with embodiment 1, and vapo(u)rizing temperature is 250 DEG C, and distillation time is 5 hours, and crude oil heated time is also 5 hours.
Test result: crude oil feeding quality 3099 grams, water quality 1630 grams deviate from by crude oil, measures crude oil water content 53.1% by GB/T8929 detecting crude oil water content method, and dewatered oil water content is 1.0 mass %, and it is 99.0 mass % that calculating obtains dehydration of crude oil rate.
By test result in above-described embodiment 1 to 3 and comparative example 1 it can be seen that adopt crude oil continuous still dehydration device of the present invention that crude oil is carried out distillation dehydration, dehydration rate is apparently higher than common method of the prior art. And device provided by the present invention can continuous feed dehydration, feedstock amount can be adjusted as required, in still-process light, heavy oil discharging time is all very short, only 5-7 minute, can being prevented effectively from the decomposition that heavy oil causes in dehydration owing to being heated, after dehydration, gained crude oil sample character is substantially free of generation thermal change.
The preferred embodiment of the present invention is described in detail above in association with accompanying drawing; but; the present invention is not limited to the detail in above-mentioned embodiment; in the technology concept of the present invention; technical scheme can being carried out multiple simple variant, these simple variant belong to protection scope of the present invention.
It is further to note that, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, it is possible to be combined by any suitable mode, in order to avoid unnecessary repetition, various possible compound modes are no longer illustrated by the present invention separately.
Additionally, can also carry out combination in any between the various different embodiment of the present invention, as long as it is without prejudice to the thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (15)
1. a crude oil continuous still dewatering, it is characterized in that, the method includes the feed duct line (31) that wet crude passes into crude oil continuous still dehydration device charging conveying assembly (30) continuously, enter back into the pipeline (21) that preheats preheating in assembly (20) to preheat, distill subsequently into the housing in housing unit (11), water and light oil in crude oil are discharged from housing upper gaseous phase outlet, reclaim through distillation gas and enter light oil and water storage tank (52) after assembly (50) condensation, water therein is discharged from light oil and water storage tank (52) bottom, carburet hydrogen is 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, reclaims through heavy oil and enters heavy oil recycling can (42) after assembly (40) condensation.
2. method according to claim 1, wherein, described charging conveying assembly (30) including:
Described feed duct line (31), its end with preheat in assembly (20) described in preheat pipeline (21) and be connected;
3rd heater (32), is used for adjusting the temperature that described feed duct line (31) is internal, it is preferable that described 3rd heater (32) is the Acanthopanan trifoliatus (L.) Merr. hot jacket being wrapped in described feed duct line (31) periphery.
3. method according to claim 2, wherein, described charging conveying assembly (30) also includes controllable temperature feed pump (33), and described controllable temperature feed pump (33) is arranged on described feed duct line (31).
4. method according to claim 1, wherein, described feed duct line (31) including:
Feeding line (311), which is provided with the feed(raw material)inlet being positioned at top, is positioned at tapping valve (313) and the leakage fluid dram (314) of bottom and superposed controllable temperature feed pump (33);
Feed-line (312), one end is connected on described feeding line (311), and be positioned between described controllable temperature feed pump (33) and described tapping valve (313), the other end be connected to described in preheat on pipeline (21)
Described wet crude from described feeding line (311) continuously into described crude oil continuous still dehydration device.
5. method according to claim 2, wherein, passes into wet crude in the process of crude oil continuous still dehydration device continuously, and the temperature controlling described 3rd heater is 20��100 DEG C.
6. preheat assembly (20) described in accordance with the method for claim 1, wherein, to include:
Described preheating pipeline (21), the arrival end being positioned at middle part with described housing is connected,
Secondary heater (22), is used for described in adjusting preheating the temperature that pipeline (21) is internal, it is preferable that described secondary heater (22) adds hot jacket for preheating the second of pipeline (21) periphery described in being wrapped in.
7. method according to claim 6, wherein, passes in the process of crude oil continuous still dehydration device continuously by wet crude, and the temperature controlling secondary heater is 100��300 DEG C.
8. method according to claim 1, wherein, described housing unit (11) including:
Described housing, is provided with arrival end in the middle part of it, top sets described gaseous phase outlet, and bottom sets liquid-phase outlet;
Upper cover (113), the open top with described housing is tightly connected;
Low head (114), is tightly connected with the bottom opening of described housing;
Described housing unit (11) is provided with primary heater (12), described primary heater (12) is for adjusting the temperature of described enclosure interior, it is preferable that described primary heater (12) adds hot jacket for being wrapped in the first of described housing periphery.
9. method according to claim 1, wherein, described in preheat pipeline (21) and extend downwardly and be connected with described housing inlet port end deviateing horizontal plane 5 �㡫30 ��.
10. method according to claim 1, wherein, described distillation gas reclaims assembly (50) and including:
Second cooling assembly (51), one end is connected with the gaseous phase outlet of described housing unit (11) housing;
Light oil and water storage tank (52), be connected with described second other end lowering the temperature assembly (51), and described light oil and water storage tank (52) be provided with gaseous phase outlet;
Carburet hydrogen recycling can (53), is connected with the gaseous phase outlet of described light oil and water storage tank (52).
11. method according to claim 10, wherein, heavy oil reclaims assembly (40) and including:
First cooling assembly (41), one end is connected with the liquid-phase outlet of described housing unit (11) housing;
Heavy oil recycling can (42), is connected with described first other end lowering the temperature assembly (41).
12. the method according to claim 10 or 11, wherein, described first cooling assembly (41) or described second cooling assembly (51) including:
Interior pipe (411), one end is connected with the liquid-phase outlet of described housing unit (11) housing, and the other end is connected with described heavy oil recycling can (42);
Outer tube (412), is wrapped in the periphery of said inner tube (411), forms temperature-reducing medium flowing lumen (413) between described outer tube (412) and said inner tube (411).
13. the method according to claim 10 or 11, wherein, the bottom of described heavy oil recycling can (42) is provided with draining valve (421) and oil drain out (422); The bottom of described light oil and water storage tank (52) is provided with drain valve (521) and discharge outlet (522); The top of described carburet hydrogen recycling can (53) is provided with air bleeding valve (532) and air vent (533).
14. method according to claim 10, wherein, when adopting distillation gas to reclaim assembly (50) condensation water from the crude oil that housing upper gaseous phase outlet is discharged and light oil, the temperature controlling the second cooling assembly (51) and light oil and water storage tank (52) is 1��15 DEG C, and the temperature of carburet hydrogen recycling can (53) is-80��-100 DEG C.
15. method according to claim 11, wherein, when adopting heavy oil to reclaim assembly (40) condensation heavy oil from the crude oil that lower housing portion liquid-phase outlet is discharged, the temperature controlling the first cooling assembly (41) and heavy oil recycling can (42) is 20��100 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410584023.1A CN105623706B (en) | 2014-10-27 | 2014-10-27 | Crude oil continuous still dewatering |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410584023.1A CN105623706B (en) | 2014-10-27 | 2014-10-27 | Crude oil continuous still dewatering |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105623706A true CN105623706A (en) | 2016-06-01 |
| CN105623706B CN105623706B (en) | 2017-07-25 |
Family
ID=56039065
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410584023.1A Active CN105623706B (en) | 2014-10-27 | 2014-10-27 | Crude oil continuous still dewatering |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105623706B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113862080A (en) * | 2021-10-18 | 2021-12-31 | 怀化市富源油业有限公司 | Tea-seed oil dewatering device |
Citations (6)
| 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 |
| 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 |
-
2014
- 2014-10-27 CN CN201410584023.1A patent/CN105623706B/en active Active
Patent Citations (6)
| 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 |
| 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 |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113862080A (en) * | 2021-10-18 | 2021-12-31 | 怀化市富源油业有限公司 | Tea-seed oil dewatering device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105623706B (en) | 2017-07-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| FI85158C (en) | Asphalt Coking Process | |
| CN113195070A (en) | Process and apparatus for cleaning contaminated waste oils | |
| RU2470064C2 (en) | Method of decelerated carbonisation of oil residues | |
| US9714388B1 (en) | Method for recycling liquid waste | |
| CN105623706A (en) | Crude oil continuous distillation and dehydration method | |
| WO2014035280A1 (en) | Method for the retarded coking of petroleum residues | |
| CN105623707A (en) | Continuous distillation dewatering device and crude oil continuous distillation dewatering device | |
| RU2683267C1 (en) | Installation for processing liquid hydrocarbons | |
| US1877811A (en) | Process for treating crude oil | |
| US8784648B2 (en) | Method for producing vacuum in a vacuum oil-stock distillation column and a plant for carrying out the method | |
| RU2759496C1 (en) | Installation for stabilization, topping and dehydration of oil | |
| AU2019217861A1 (en) | Apparatus and method for a remediation plant | |
| US1904213A (en) | Method and apparatus for distilling oil | |
| CN103657264B (en) | Remove recycle hydrogen drop and the devices and methods therefor of granule in hydrogenated pyrolysis gasoline | |
| RU2106388C1 (en) | Crude oil treatment installation | |
| RU67088U1 (en) | UNIT AND EVAPORATION UNIT FOR PREPARATION OF OIL AND OTHER HYDROCARBON MEDIA | |
| RU2263702C1 (en) | Liquid hydrocarbon medium distillation process | |
| US1917895A (en) | Method and apparatus for condensing and purifying vapors and gases | |
| RU2513857C1 (en) | Method for integrated processing of oil-containing stock | |
| RU2137803C1 (en) | Oil stock distillation process | |
| RU2176262C2 (en) | Method of gasoline production | |
| CN114891531A (en) | Method for removing aromatic hydrocarbon in straight-run naphtha | |
| RU41306U1 (en) | DEVICE FOR SEPARATION OF OIL AND OTHER HYDROCARBON MEDIA | |
| RU2264431C1 (en) | Crude oil processing method | |
| RU2165957C2 (en) | Gasoline production process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |