CN204767628U - High -pressure separator of multiple optimization - Google Patents
High -pressure separator of multiple optimization Download PDFInfo
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- CN204767628U CN204767628U CN201520378743.2U CN201520378743U CN204767628U CN 204767628 U CN204767628 U CN 204767628U CN 201520378743 U CN201520378743 U CN 201520378743U CN 204767628 U CN204767628 U CN 204767628U
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Abstract
The utility model provides a high -pressure separator of multiple optimization which the draw ratio is 2.5-5.5: 1, the feed inlet is located the barrel side, and more than the liquid level, liquid level is 10%-50% of barrel tangential length, and feed inlet central line to barrel medium line is the 15% -40% of barrel tangential length, under the heavy ends discharge gate was located the high -pressure separator barrel, the light component discharge gate set up in the barrel top, cylinder bottom adopts the conical body structure to the part of heavy ends discharge gate, and the cone angle is 40 -120. The utility model is suitable for a more vrds technology, coal direct liquefaction process and the mixing technology of oily coal of solids content under the environment of higher operating pressure, applicable operating temperature scope is great to can realize fine separation effect, the coking rate is low just can not remained.
Description
Technical field
The utility model relates to a kind of high-pressure separator and separation method thereof of Multiple Optimization, belongs to petrochemical industry and coal chemical technology.
Background technology
In recent years, along with the continuous increase of global crude oil yield and the continuous minimizing of conventional crude reserves, crude oil in poor quality trend is more and more serious, and meanwhile, the demand of market to light oil constantly increases.So, heavy-oil slurry hydrogenation technique, direct coal liquefaction process and coal calendering process more and more come into one's own, this several technology all needs to adopt one high-pressure separator efficiently, this equipment is arranged on paste state bed reactor downstream, material from paste state bed reactor outlet enters separator, weight component is separated at this, light component enters the separator of the low one-level of temperature, heavy constituent enters the separator of the low one-level of pressure, continue to be separated, until the recycle hydrogen in light component realizes being separated with oil gas, solid phase in heavy constituent, oil and water realize being separated, so, separator, especially high-pressure separator becomes one of nucleus equipment of aforementioned several technique, its stability is related to recycle hydrogen system, fractionating system, light ends unit, exhaust gas processing device, the operational stability of wastewater treatment equipment etc.
The common separator of current oil plant or coal plant is generally process gas-liquid two-phase medium, because object realizes gas-liquid separation nothing more than, so structure is relatively simple.Because the common feature of heavy-oil hydrogenation, DCL/Direct coal liquefaction and the mixing reactor of oily coal is HTHP, reactor outlet material component is complicated, also comprise many solids, except the piece-rate system considering to use multicomponent to form from device, also to carry out particular design to separator, especially high-pressure separator.When the operating temperature of high-pressure separator is higher, also easily there is coking phenomenon, equipment is caused to block, even to blast accident, so need to accomplish to avoid coking as far as possible, also will possess the function of in time process coking material, the operation medium of the separator of the mixing and oily coal calendering process of heavy-oil slurry hydrogenation, oily coal is gas-liquid-solid three-phase medium, needs special structural design simultaneously.In addition, high-pressure separator is the gas-liquid separation equipment of product, is again the pressure control point of reaction system.In separator, pressure is very large, and as level control is bad, liquid level is too high, can cause Vapor Entrainment liquid phase and solid phase seriously, and cause cold exchange device to block, liquid level is too low, easy generation high-pressure system scurries into low-pressure system and accident of blasting, and adds the operation easier of high-pressure separator.
Utility model content
In order to solve the problem of prior art, the utility model provides a kind of high-pressure separator of Multiple Optimization, can realize the weight Component seperation of gas-liquid two-phase or gas-liquid-solid three-phase; Both farthest reduced the possibility of coking, and coking material can have been cleared up again in time and avoid blocking; The design of gating location, heavy constituent export structure and liquid level makes that input and output material is more unobstructed, equipment operating is convenient, equipment runs more stable.
The technical solution of the utility model:
A kind of high-pressure separator of Multiple Optimization, it is characterized in that high-pressure separator draw ratio is 2.5 ~ 5.5:1, charging aperture is positioned at cylindrical shell side, and more than liquid level, liquid level is 10% ~ 50% of cylindrical shell tangential length, and charging aperture center line to cylindrical shell medium line is the 15%-40% (i.e. charging aperture height) of cylindrical shell tangential length; Heavy constituent discharging opening is positioned at immediately below high-pressure separator cylindrical shell, and light component discharging opening is arranged on above cylindrical shell; Cylindrical shell lower end adopts taper structure to the part of heavy constituent discharging opening, and cone angle is 40-120 °.
Operating temperature is preferably 30-470 DEG C, and operating pressure is preferably 17-22MPa.
Described high-pressure separator operation medium can be gas-liquid-solid three-phase mixture.
Can also comprise hydrogen make-up entrance, described hydrogen make-up entrance is positioned at the sidepiece of bullet, and the hydrogen dividing potential drop in high-pressure separator is 8-14MPa.
The high-pressure separator attainable time of staying is: 0.5-90 minute.
Each outlet of described high-pressure separator can preferably arrange backwash mouth.
Wax oil in preferred use product or heavy diesel fuel rinse.
Technique effect:
The high-pressure separator of a kind of Multiple Optimization of the present utility model is applicable to solids content under the environment of higher operating pressure more heavy oil hydrogenation process, direct coal liquefaction process and oily coal calendering process, described heavy oil is one or more combinations of heavy crude, residual oil, catalytic slurry, de-oiled asphalt, coal tar, described coal is one or more combinations in brown coal, bituminous coal, dross coal, and in described oily coal calendering process, oil is 97:3-40:60 with the proportion of coal.The operating temperature range be suitable for is comparatively large, and can realize good separating effect; The measure of hydrogen make-up is set, can realizes at relatively high temperatures, hydrocarbon molecule not polycondensation coking; Import is arranged on cylindrical shell side instead of the upper end of ullage, can make once liquid phase generation coking is unlikely to block charging aperture, isolated generation can not be made in addition to reflux and hinder charging, the moderate range of draw ratio makes charging aperture layout convenient, and making the balance that the interface of gas-liquid separation and floor space reach good, cost is controlled; Liquid level is arranged on 15-50% scope, makes operation more stable, avoids the too high light component of liquid level and carries the too much or too low light component of liquid level of heavy constituent secretly and flow out from lower end; Be set to taper near heavy constituent discharging opening and outlet is arranged at the cone end, make the heavy constituent such as liquid-solid be guided landing to separate more efficiently, even if coking once in a while, coking material also can leave separator with heavy constituent and can not block discharging opening.
For ensureing hydrogen dividing potential drop, when operating temperature is higher than 300 DEG C, to hydrogen make-up in high-pressure separator, hydrogen dividing potential drop and high-pressure separator operating pressure and operating temperature positive correlation, hydrogen dividing potential drop is 8-14MPa.
High-pressure separator respectively exports and arranges backwash mouth, uses wax oil or heavy diesel fuel to rinse coking, coking material is cleared up timely, improves operational stability and the cycle of operation of equipment; Because backwash material is product, therefore can not introduce impurity and increase cost.
Accompanying drawing explanation
Fig. 1 is the reactor sketch of the utility model embodiment, and in figure, each label lists as follows:
1-separator main body, 2-feed pipe, 3-liquid level, 4-light component discharging opening, 5-heavy constituent discharging opening, 6-light fraction outlet backwash mouth, 7-light fraction outlet backwash mouth, 8-heavy constituent outlet backwash mouth, 9-heavy constituent outlet backwash mouth, 10-hydrogen inlet, 11-hydrogen inlet, 12-heavy constituent outlet backwash mouth, 13-heavy constituent outlet backwash mouth.
Detailed description of the invention
For setting forth specific features of the present utility model further, composition graphs 1 and specific embodiment are illustrated.
Embodiment
As shown in Figure 1, this separator is the high-temperature high-pressure separator in oily coal calendering process.
The medium entering separator main body 1 is gas-liquid-solid three-phase mixture; Separator operating temperature is 455 DEG C, and operating pressure is about 18.7MPa, and the separator designs time of staying is 2 minutes; Membrane Separator Cylinder for CFB Boiler tangential length is L=3m, and interior electrical path length is 0.25L; The charging aperture of feed pipe 2 is positioned at cylindrical shell side and more than liquid level, distance cylindrical shell top is 0.25L, and liquid level 3 is highly fluctuation (in figure, state is 3L) between 0.25-0.4L, and arranges level control heavy constituent discharge; Heavy constituent discharging opening 5 is positioned at immediately below high-pressure separator cylindrical shell, and light component discharging opening 4 is arranged on above cylindrical shell; Cylindrical shell lower end adopts taper structure to the part of heavy constituent discharging opening 5, and cone angle is 90 °.Comprise the import of hydrogen make-up, hydrogen inlet 11 is positioned at the sidepiece of bullet, and hydrogen divides pressure-controlled between 11-13MPa.Light fraction outlet backwash mouth 6,7 and heavy constituent outlet backwash mouth 8,9,12,13 are set respectively near light component discharging opening 4 and heavy constituent discharging opening 5.
The present embodiment, through long-play, under proving that it is applicable to the environment of higher operating pressure, and can realize good separating effect; The measure of hydrogen make-up is set, can realizes at relatively high temperatures, hydrocarbon molecule not polycondensation coking; The import of feed pipe 2 is arranged on cylindrical shell side instead of the upper end of ullage, can make once liquid phase generation coking is unlikely to block charging aperture, isolated generation can not be made in addition to reflux and hinder charging, the moderate range of draw ratio makes charging aperture convenient and take into account the effect of separation and the volume of equipment when arranging, thus optimized device cost; The height of liquid level 3 makes operation more stable, be unlikely to light component carry secretly heavy constituent too much or light component flow out from lower end; Be set to taper near heavy constituent discharging opening 5 and export be arranged at the cone end, the heavy constituent such as liquid-solid is made to be guided landing to separate more efficiently, even if coking once in a while, coking material also can leave separator with heavy constituent landing and can not block discharging opening; Each outlet arranges backwash point and makes coking material obtain cleaning strong in time, improves operational stability and the cycle of operation of equipment, and overall operation is very steady, does not have the residual of coking material; Use wax oil or heavy diesel fuel to rinse coking, because backwash material is product, therefore can not introduce impurity and increase cost.
The foregoing is only the utility model preferably detailed description of the invention; but protection domain of the present utility model is not limited thereto; anyly be familiar with those skilled in the art in the technical scope that the utility model discloses; the change that can expect easily or replacement, all should be encompassed within protection domain of the present utility model.Therefore, protection domain of the present utility model should be as the criterion with the protection domain of claims.
Claims (5)
1. the high-pressure separator of a Multiple Optimization, it is characterized in that high-pressure separator draw ratio is 2.5 ~ 5.5:1, charging aperture is positioned at cylindrical shell side, and more than liquid level, liquid level is 10% ~ 50% of cylindrical shell tangential length, and charging aperture center line to cylindrical shell medium line is the 15%-40% of cylindrical shell tangential length; Heavy constituent discharging opening is positioned at immediately below high-pressure separator cylindrical shell, and light component discharging opening is arranged on above cylindrical shell; Cylindrical shell lower end adopts taper structure to the part of heavy constituent discharging opening, and cone angle is 40-120 °.
2. the high-pressure separator of a kind of Multiple Optimization according to claim 1, is characterized in that described high-pressure separator operation medium is gas-liquid-solid three-phase mixture.
3. the high-pressure separator of a kind of Multiple Optimization according to claim 1, characterized by further comprising hydrogen make-up entrance, and described hydrogen make-up entrance is positioned at the sidepiece of bullet, and the hydrogen dividing potential drop in high-pressure separator is 8-14MPa.
4. the high-pressure separator of a kind of Multiple Optimization according to claim 1, is characterized in that each outlet of described high-pressure separator arranges backwash mouth.
5. the high-pressure separator of a kind of Multiple Optimization according to claim 4, is characterized in that using the wax oil in product or heavy diesel fuel to rinse.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520378743.2U CN204767628U (en) | 2015-06-03 | 2015-06-03 | High -pressure separator of multiple optimization |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520378743.2U CN204767628U (en) | 2015-06-03 | 2015-06-03 | High -pressure separator of multiple optimization |
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| CN204767628U true CN204767628U (en) | 2015-11-18 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104888500A (en) * | 2015-06-03 | 2015-09-09 | 北京中科诚毅科技发展有限公司 | Multi-optimized high pressure separator |
| CN116410788A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Poor-quality heavy oil slurry bed hydrocracking treatment equipment and treatment method |
-
2015
- 2015-06-03 CN CN201520378743.2U patent/CN204767628U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104888500A (en) * | 2015-06-03 | 2015-09-09 | 北京中科诚毅科技发展有限公司 | Multi-optimized high pressure separator |
| CN116410788A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Poor-quality heavy oil slurry bed hydrocracking treatment equipment and treatment method |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170720 Address after: 215311, Kunshan, Jiangsu Province, Xueyuan Road Town, No. 88, 1 Patentee after: Kunshan super clean energy Co., Ltd. Address before: 100098 Beijing city Haidian District Dazhongsi Hospital No. 13, No. 1 building, Lou Huajie B219 Patentee before: Zhongke Chuangyi Tech Development Co., Ltd. |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190425 Address after: 100098 Huajie Building B219, Building 1, 13 Dazhong Temple, Haidian District, Beijing Patentee after: Zhongke Chuangyi Tech Development Co., Ltd. Address before: 215311 No. 88 Bacheng College Road, Kunshan City, Jiangsu Province Patentee before: Kunshan super clean energy Co., Ltd. |
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| TR01 | Transfer of patent right |