CN103920541A - Boiling-bed hydrogenation catalyst de-oiling system and method thereof - Google Patents
Boiling-bed hydrogenation catalyst de-oiling system and method thereof Download PDFInfo
- Publication number
- CN103920541A CN103920541A CN201310016047.2A CN201310016047A CN103920541A CN 103920541 A CN103920541 A CN 103920541A CN 201310016047 A CN201310016047 A CN 201310016047A CN 103920541 A CN103920541 A CN 103920541A
- Authority
- CN
- China
- Prior art keywords
- gas
- oil
- oiling
- catalyst
- tank
- 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.)
- Pending
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a boiling-bed hydrogenation catalyst de-oiling system. The system comprises a catalyst de-oiling unit, an oil-gas separation unit and a gas post-processing cycling unit; the catalyst de-oiling unit comprises a regeneration catalyst de-oiling tank (1), the top of the tank is provided with a regeneration catalyst (10) inlet, a pipeline at the inlet is provided with a recycle gas (16) inlet, and the bottom of the tank is provided with an oil-containing material flow (17) outlet; the oil-gas separation unit comprises an oil-gas separator (5), the top of the separator is provided with a liquid-gas (13) outlet, and the bottom of the separator is provided with an oil product (20) outlet; the gas post-processing cycling unit comprises a gas post-processing device (6), the upper part of the device is provided with a liquid-containing gas (13) inlet, the top of the device is provided with a liquid-removed gas (12) outlet which is connected with a recycle gas inlet pipeline of the regeneration catalyst de-oiling tank (1); and the recycle gas inlet pipeline is provided with a supplement gas (11) inlet and a gas cycling machine (7), and the recycle gas inlet pipeline is successively connected with a heat exchanger (3) shell side and a heater (2) for forming a gas cycling loop. The invention discloses a method for collecting separated oil products and performing cyclic utilization on gas in the system.
Description
Technical field
A kind of catalyst de-oiling technology that the present invention relates to petrochemical industry and Coal Chemical Industry industry, particularly, the present invention relates to a kind of boiling bed hydrogenation catalyst de-oiling system and method thereof.
Background technology
Boiling bed residual oil hydrogen addition technology is the important technology of processing high-sulfur, high carbon residue, high metal mink cell focus, and for solving, fixed bed residual hydrogenation air speed is low, catalysqt deactivation is fast, system pressure drop is large, easily coking, install the problems such as the cycle of operation is short and have clear superiority.Boiling bed hydrogenation technology is because reactor temperature is even, grow, install flexible operation service cycle, in commercial Application, obtain increasing concern, since two thousand external newly-built boiling bed residual oil hydrocracking device is more than fixed bed residual hydrogenation equipment, to meet the needs of heavy crude oil depth processing inferior.
Domestic boiling bed residual oil hydrogenation is in introducing and the independent development stage, and the boiling bed hydrogenation of Shenhua Group liquefied coal coil adopts the T-Star technology of AXENS, and since driving in December, 2008, running always so far.Sinopec adopts the boiling bed hydrogenation technology of independent intellectual property right exploitation to build a set of 50,000 tons/year of boiling bed residual oil hydrocracking Industrial demonstration devices in Nanjing petrochemical industry branch company, be installed on and go into operation for the end of the year 2013, after success of the test, by building a collection of boiling bed residual oil hydrogenation plant with independent intellectual property right, replace gradually traditional coking plant.One of distinguishing feature of boiling bed hydrogenation be catalyst add online row's (being that catalyst is changed online), be 0.1-0.9kg/ ton feedstock oil according to the different catalysts replacement amount of feedstock property, the dead catalyst oil content drawing off is up to 20-50wt%, in order to prevent that overheating problem from appearring in the catalyst coke burning regeneration initial stage, before catalyst regeneration, must carry out on the spot de-oiling processing.
Chinese invention patent CN1298925 discloses a kind of external regeneration process of hydrogenating catalyst, it adds vertical thin layer moving bed regenerator by catalyst by top, pass through successively preheating section, sulphur burning step, charcoal burning step and cooling section, carry out respectively preheating de-oiling, desulfurization, de-charcoal and cooling, cooled regenerated catalyst is discharged by regenerator.But above-mentioned technique is not collected the oil product removing, and also gas is not recycled.
In sum, the method for existing recovery boiling bed hydrogenation catalyst is not processed the contained oil product of catalyst, also gas is not wherein processed, and cannot recycle oil product and gas.
Summary of the invention
The problem that cannot recycle the contained oil product of catalyst and gas for the method for existing recovery catalyst, the invention provides a kind of boiling bed hydrogenation catalyst de-oiling system and method thereof.The method comprises and separates the step that reclaims the contained oil product of catalyst and gas circulation is utilized, and solved in existing boiling bed hydrogenation catalyst recovery method the problem that cannot recycle oil product and gas.
An object of the present invention is to provide a kind of boiling bed hydrogenation catalyst de-oiling system.
A kind of boiling bed hydrogenation catalyst de-oiling system of the present invention, comprises catalyst de-oiling unit, Oil-gas Separation unit and gas post processing cycling element.
Described catalyst de-oiling unit comprises regenerated catalyst de-oiling tank 1, and its top arranges regenerated catalyst 10 entrances, is provided with recyclegas 16 entrances on the pipeline of regenerated catalyst 10 entrances, and its bottom arranges oil-containing logistics 17 and exports.
Described Oil-gas Separation unit comprises gs-oil separator 5, and its top arranges containing liquid gas 13 and exports, and its bottom is provided with oil product 20 and exports, and is connected with oil product collecting tank 8; Gs-oil separator 5 tops are provided with oil-containing logistics 17 entrances and are connected with oil-containing logistics 17 outlet lines of regenerated catalyst de-oiling tank 1 bottom, and this pipeline, by heat exchanger 3 tube sides, is provided with cooler 4 afterwards on it.
Described gas post processing cycling element comprises gas preprocessor 6, and its top is provided with containing liquid gas 13 entrances, with being connected containing liquid gas 13 outlet lines of gs-oil separator 5 tops; These gas preprocessor 6 tops arrange de-liquid gas 12 and export, and it is connected with recyclegas 16 suction lines on regenerated catalyst 10 suction lines of catalyst de-oiling regeneration unit catalyst de-oiling tank 1; On this pipeline, be provided with make-up gas 11 entrances, gas circulation machine 7, this pipeline, by heat exchanger 3 shell sides, is provided with heater 2 after this afterwards, forms gas circulation loop.Described gas preprocessor 6 all carries out gas-liquid separation with described gs-oil separator 5, in described gs-oil separator 5, isolate a large amount of liquid, entering before compressor to pass through gas preprocessor 6 separating liquid again, in described gas preprocessor 6, isolate micro liquid.The material interruption of gas preprocessor 6 outlet at bottoms enters underground sump oil pipe network.
Recyclegas 16 entrances on regenerated catalyst 10 suction lines of described regenerated catalyst de-oiling tank 1 can be selected various existing gas distributors in prior art, preferably, recyclegas 16 entrances are provided with circular rings tubular gas distributor conventional on refining device.Regenerated catalyst 10 flows in regenerated catalyst de-oiling tank 1 in the ring of this gas distributor, and 16 of recyclegas can be uniformly distributed at whole regenerated catalyst de-oiling tank 1 interface energy, are conducive to de-oiling.Catalyst is after de-oiling, and its oil content is not more than 3wt%, can meet the oil content requirement of catalyst regeneration.
Described gs-oil separator 5 can adopt existing general gas-liquid separation inner member in prior art, preferably adopts eddy flow to take off liquid pipe group.The micro vortex flow tube group providing in the de-liquid Guan Zuwei Chinese patent ZL200810201687.X of described eddy flow.This micro vortex flow tube group has commercially available prod at present, and selling producer is that Shanghai Hua Chang equipment development Co., Ltd model is: HL/G.20 microns of can ensure that gas carries secretly of the micro vortex flow tube group adopting and above drop removal efficiency exceed 99%.
In order to take out the convenient catalyst of having regenerated, preferably, in system of the present invention, regenerated catalyst de-oiling tank 1 adopts flange connection, convenient mounting or dismounting.In addition, after the catalyst regeneration in regenerated catalyst de-oiling tank 1, also can take out (conventionally drawing off from regenerated catalyst de-oiling tank 1 bottom) by taking flange apart, more convenient.
In order to prevent that the gas trains in gs-oil separator 5 from arriving in oil product collecting tank 8, preferably, on described gs-oil separator 5, be provided with liquid level controller 32, between gs-oil separator 5 and oil product collecting tank 8, be provided with Liquid level adjusting valve, control the unlatching of Liquid level adjusting valve by the liquid level controller 32 being arranged on gs-oil separator 5, thereby control the conveying of liquid between described gs-oil separator 5 and described oil product collecting tank 8.By the level condition in monitoring gs-oil separator 5, control the opening degree of Liquid level adjusting valve, realize the amount for its isolated liquid input oil product collecting tank 8.For example, in gs-oil separator 5 during without liquid level, Liquid level adjusting valve standard-sized sheet, now gas just string in oil product collecting tank 8, for the anti-situation of planting here, arrive certain low liquid level in the interior liquid level of gs-oil separator 5, while accounting for gs-oil separator 5 cumulative volume 10% such as liquid level, just close Liquid level adjusting valve.When the liquid level of gs-oil separator 5 is higher, when reaching gs-oil separator 5 cumulative volume 70%, open outlet regulating valve; Control with this amount that liquid (oil product 20) enters oil product collecting tank 8.Described oil product collecting tank 8 discharging openings are connected to pump 9 with by final oil product 21 transmitting systems.
In order to make the recyclegas 16 that enters regenerated catalyst de-oiling tank 1 be beneficial to de-oiling in suitable temperature range, before recyclegas 16 entrances of described regenerated catalyst de-oiling tank 1, be provided with the second temperature controller 30; In order to make the oil-containing material that enters gs-oil separator 5 be beneficial to Oil-gas Separation in suitable temperature range, the first temperature controller 31 is set before oil-containing logistics 17 entrances of gs-oil separator 5.
Described regenerated catalyst de-oiling tank 1 also can serve as the dead catalyst storage tank in boiling bed hydrogenation technique system, or outside regenerated catalyst de-oiling tank 1, connect dead catalyst storage tank, need the reliable gravity inflow of the dead catalyst regenerated catalyst de-oiling tank 1 of regeneration to carry out de-oiling.
Another object of the present invention is to provide a kind of method of boiling bed hydrogenation catalyst de-oiling.
The method of a kind of boiling bed hydrogenation catalyst de-oiling of the present invention, the system of employing the invention described above, it comprises the following steps:
Regenerated catalyst 10 is intermittently delivered to de-oiling in regenerated catalyst de-oiling tank 1 and form oil-containing logistics 17, in system de-liquid gas 12 together with make-up gas 11 after gas circulation machine 7 boosts with oil-containing logistics 17 through heat exchanger 3 heat exchange, carry out gas-liquid separation by the cooling gs-oil separator 5 that enters of cooler 4, the isolated oil product 20 of gs-oil separator 5 enters oil product collecting tank 8; This gs-oil separator 5 is isolated to be removed liquid containing liquid gas 13 by gas preprocessor 6 and forms de-liquid gas 12, boost by gas circulation machine 7 with make-up gas 11 afterwards and after 3 li, heat exchanger and oil-containing logistics 17 heat exchange, return catalizer regenerated catalyst de-oiling tank 1 after heating up by heater 2.
Described gas of the present invention, comprises make-up gas 11, recyclegas 16, and above-mentioned gas is inert gas, can adopt nitrogen, helium, argon gas, preferred nitrogen.
In order to make the oil-containing material that enters gs-oil separator 5 be beneficial to Oil-gas Separation in suitable temperature range, the oil-containing logistics 17 of gs-oil separator 5, is cooled to 40 ~ 55 DEG C by the temperature of the oil-containing logistics 17 that enters described gs-oil separator 5 through heat exchange; In order to make the recyclegas 16 that enters regenerated catalyst de-oiling tank 1 be beneficial to de-oiling in suitable temperature range, the recyclegas 16 that enters regenerated catalyst de-oiling tank 1 is heated to 250 ~ 300 DEG C through heat exchange.Above temperature range is monitored by temperature controller.
Described gs-oil separator 5 oil product 20 out enters oil product collecting tank 8 by Liquid level adjusting valve, and controls the unlatching of Liquid level adjusting valve by liquid level controller 32.
Pass through pump 9 by final oil product 21 transmitting systems from described oil product collecting tank 8.
Described regenerated catalyst de-oiling tank 1 interior operating temperature is 250 ~ 300 DEG C, and operating pressure is 0.7 ~ 0.8MPa (G), gas agent volume ratio, and gas standard volume is not less than 300:1 with catalyst volume ratio, and the scope of gas agent volume ratio is 300:1 ~ 800:1.The interior operating temperature of described gs-oil separator 5 is not higher than 55 DEG C, and preferably 40 ~ 55 DEG C, operating pressure is 0.4 ~ 0.5MPa (G), and the pressure in present specification and claims is meter pressure, the Mpa of unit (G).
In addition also can affect catalyst de-oiling rate the duration of runs that, in method of the present invention, gas circulation machine 7 is processed every batch of catalyst.So can adjust according to catalyst oil content the duration of runs of described gas circulation machine 7, oil content is high, the duration of runs of gas circulation machine 7 is long, to ensure the de-oiling effect of catalyst.The a collection of catalyst of general processing, be 8 ~ 24 hours the duration of runs of gas circulation machine 7, preferably 8 hours.
The system and method for a kind of boiling bed hydrogenation catalyst de-oiling provided by the present invention, isolated oil product can be collected, and the gas circulation utilization that de-oiling is adopted, realize the recycling of oil product and gas, through the catalyst of process de-oiling of the present invention, its oil content is not more than 3wt%.
Brief description of the drawings
Accompanying drawing 1 is system and the schematic flow sheet of boiling bed hydrogenation catalyst de-oiling of the present invention.
Description of reference numerals:
1 regenerated catalyst de-oiling tank, 2 heaters, 3 heat exchangers, 4 coolers, 5 gs-oil separators, 6 gas preprocessors, 7 gas circulation machines, 8 oil product collecting tanks, 9 pumps, 10 regenerated catalysts, 11 make-up gas, 12 de-liquid gases, 13 are containing liquid gas, 16 recyclegas, 17 oil-containing logistics, 20 oil products, 21 final oil products, 30 second temperature controllers, 31 first temperature controllers, 32 liquid level controllers.
Detailed description of the invention
Below in conjunction with embodiment, further illustrate the present invention.
A kind of boiling bed hydrogenation catalyst de-oiling system of the present invention and method thereof, described system comprises catalyst de-oiling unit, Oil-gas Separation unit and gas post processing cycling element.Described catalyst de-oiling unit comprises regenerated catalyst de-oiling tank 1, and its top arranges regenerated catalyst 10 entrances, is provided with recyclegas 16 entrances on the pipeline of regenerated catalyst 10 entrances, and its bottom arranges oil-containing logistics 17 and exports; Described Oil-gas Separation unit comprises gs-oil separator 5, and its top arranges containing liquid gas 13 and exports, and its bottom is provided with oil product 20 and exports, and is connected with oil product collecting tank 8; Gs-oil separator 5 tops are provided with oil-containing logistics 17 entrances and are connected with oil-containing logistics 17 outlet lines of regenerated catalyst de-oiling tank 1 bottom, and this pipeline, by heat exchanger 3 tube sides, is provided with cooler 4 afterwards on it; Described gas post processing cycling element comprises gas preprocessor 6, and its top is provided with containing liquid gas 13 entrances, with being connected containing liquid gas 13 outlet lines of gs-oil separator 5 tops; These gas preprocessor 6 tops arrange de-liquid gas 12 and export, and it is connected with the recyclegas suction line on regenerated catalyst 10 suction lines of catalyst de-oiling regeneration unit catalyst de-oiling tank 1; On this pipeline, be provided with make-up gas 11 entrances, gas circulation machine 7, this pipeline, by heat exchanger 3 shell sides, is provided with heater 2 after this afterwards, forms thus gas circulation loop.
Recyclegas 16 entrances on described regenerated catalyst de-oiling tank 1 regenerated catalyst 10 suction lines are provided with circular rings tubular gas distributor.The gas-liquid separation inner member that described gs-oil separator 5 adopts is the de-liquid pipe group of eddy flow, and its model is: HL/G, selling producer is Shanghai Hua Chang equipment development Co., Ltd.Described regenerated catalyst de-oiling tank 1 adopts flange connection.On described gs-oil separator 5, be provided with liquid level controller 32, between gs-oil separator 5 and described oil product collecting tank 8, be provided with the Liquid level adjusting valve of being controlled by liquid level controller 32.The first temperature controller 31 is set before oil-containing logistics 17 entrances of described gs-oil separator 5, before the recyclegas entrance of described regenerated catalyst de-oiling tank 1, is provided with the second temperature controller 30.Described oil product collecting tank 8 discharging openings are connected to pump 9 with by final oil product 21 transmitting systems.
Method of the present invention is specific as follows:
The regenerated catalyst of oil-containing 30wt% 10 is intermittently delivered to de-oiling in regenerated catalyst de-oiling tank 1 and form oil-containing logistics 17, in system de-liquid gas 12 together with make-up gas 11 after gas circulation machine 7 boosts with oil-containing logistics 17 through heat exchanger 3 heat exchange, carry out gas-liquid separation by the cooling gs-oil separator 5 that enters of cooler 4, the isolated oil product 20 of gs-oil separator 5 enters oil product collecting tank 8; This gs-oil separator 5 is isolated to be removed liquid containing liquid gas 13 by gas preprocessor 6 and forms de-liquid gas 12, boost by gas circulation machine 7 with make-up gas 11 afterwards and after 3 li, heat exchanger and oil-containing logistics 17 heat exchange, return catalizer regenerated catalyst de-oiling tank 1 after heating up by heater 2.Described gs-oil separator 5 oil product 20 is out by entering oil product collecting tank 8 by the Liquid level adjusting valve of tank gage control.Pass through pump 9 by final oil product 21 transmitting systems from described oil product collecting tank 8.
The temperature of the oil-containing logistics 17 that enters described gs-oil separator 5 is cooled to 40 ~ 55 DEG C through heat exchange; The recyclegas that enters regenerated catalyst de-oiling tank 1 is heated to 250 ~ 300 DEG C through heat exchange.
The operating temperature of regenerated catalyst de-oiling tank 1 is 250 ~ 300 DEG C, and operating pressure is 0.7 ~ 0.8MPa (G), is (300 ~ 800) at gas standard volume with catalyst volume ratio: 1 time operation.
The operating temperature of gs-oil separator 5 is 40 ~ 50 DEG C, and operating pressure is 0.4MPa (G).
Be 8 ~ 24 hours the duration of runs that described gas circulation machine 7 is processed every batch of catalyst, preferably 8 hours.Adjust the duration of runs of gas circulation machine 7 according to catalyst oil content, and oil content is high, and the duration of runs of gas circulation machine 7 is long, and in the process of its running, rotating speed is constant.
Process of the present invention is applicable to domestic boiling bed hydrogenation device catalyst, the catalyst after de-oiling, and its oil content is not more than 3wt%.
Claims (15)
1. a boiling bed hydrogenation catalyst de-oiling system, comprises catalyst de-oiling unit, it is characterized in that:
Described system also comprises Oil-gas Separation unit and gas post processing cycling element;
Described catalyst de-oiling unit comprises regenerated catalyst de-oiling tank (1), and its top arranges regenerated catalyst (10) entrance, is provided with recyclegas (16) entrance on the pipeline of regenerated catalyst (10) entrance, and its bottom arranges oil-containing logistics (17) outlet;
Described Oil-gas Separation unit comprises gs-oil separator (5), and its top arranges containing liquid gas (13) outlet, and its bottom is provided with oil product (20) outlet, is connected with oil product collecting tank (8); Gs-oil separator (5) top is provided with oil-containing logistics (17) entrance and is connected with oil-containing logistics (17) outlet line of regenerated catalyst de-oiling tank (1) bottom, and this pipeline, by heat exchanger (3) tube side, is provided with cooler (4) afterwards on it;
Described gas post processing cycling element comprises gas preprocessor (6), and its top is provided with containing liquid gas (13) entrance, with being connected containing liquid gas (13) outlet line of gs-oil separator (5) top; This gas preprocessor (6) top arranges de-liquid gas (12) outlet, and it is connected with the recyclegas suction line on regenerated catalyst (10) suction line of catalyst de-oiling regeneration unit catalyst de-oiling tank (1); On this pipeline, be provided with make-up gas (11) entrance, this entrance is connected with gas circulation machine (7), and this pipeline, by heat exchanger (3) shell side, is provided with heater (2) after this afterwards, forms thus gas circulation loop.
2. system according to claim 1, is characterized in that:
Recyclegas (16) entrance on described regenerated catalyst de-oiling tank (1) regenerated catalyst (10) suction line is provided with circular rings tubular gas distributor.
3. system according to claim 1, is characterized in that:
The gas-liquid separation inner member that described gs-oil separator (5) adopts is the de-liquid pipe group of eddy flow.
4. system according to claim 1, is characterized in that:
Described regenerated catalyst de-oiling tank (1) adopts flange connection.
5. system according to claim 1, is characterized in that:
On described gs-oil separator (5), be provided with liquid level controller (32), between gs-oil separator (5) and described oil product collecting tank (8), be provided with the Liquid level adjusting valve of being controlled by liquid level controller (32).
6. system according to claim 1, is characterized in that:
The first temperature controller (31) is set before described gs-oil separator (5) oil-containing logistics (17) entrance, before described regenerated catalyst de-oiling tank (1) recyclegas entrance, is provided with the second temperature controller (30).
7. system according to claim 1, is characterized in that:
Described oil product collecting tank (8) discharging opening is connected to pump (9) with by final oil product (21) transmitting system.
8. system according to claim 1, is characterized in that:
Recyclegas entrance on regenerated catalyst (10) suction line of described regenerated catalyst de-oiling tank (1) is provided with circular rings tubular gas distributor;
The gas-liquid separation inner member that described gs-oil separator (5) adopts is the de-liquid pipe group of eddy flow;
Described regenerated catalyst de-oiling tank (1) adopts flange connection;
Between described gs-oil separator (5) and described oil product collecting tank (8), be provided with liquid level controller (32);
Before described gs-oil separator (5) oil-containing logistics (17) entrance, be provided with the first temperature controller (31), before described regenerated catalyst de-oiling tank (1) recyclegas entrance, be provided with the second temperature controller (30);
Described oil product collecting tank (8) discharging opening is connected to pump (9) with by final oil product (21) transmitting system.
9. a de-oiling method for the boiling bed hydrogenation catalyst de-oiling system of use as described in claim 1 to 8 any one, it comprises the following steps:
Regenerated catalyst (10) is intermittently delivered to de-oiling in regenerated catalyst de-oiling tank (1) and form oil-containing logistics (17), in system de-liquid gas (12) together with make-up gas (11) after gas circulation machine (7) boosts with oil-containing logistics (17) through heat exchanger (3) heat exchange, carry out gas-liquid separation by the cooling gs-oil separator (5) that enters of cooler (4), the isolated oil product of gs-oil separator (5) (20) enters oil product collecting tank (8); This gs-oil separator (5) isolated containing liquid gas (13) by gas preprocessor (6) remove liquid form take off liquid gas (12), boost by gas circulation machine (7) with make-up gas (11) afterwards and heat exchanger (3) inner with oil-containing logistics (17) heat exchange after, by heater (2) heat up after return catalizer regenerated catalyst de-oiling tank (1).
10. method according to claim 9, is characterized in that:
The temperature of the oil-containing logistics (17) that enters described gs-oil separator (5) is cooled to 40 ~ 55 DEG C through heat exchange; The recyclegas that enters regenerated catalyst de-oiling tank (1) is heated to 250 ~ 300 DEG C through heat exchange; Monitor described temperature range by temperature controller.
11. methods according to claim 9, is characterized in that:
Described gs-oil separator (5) oil product (20) out enters oil product collecting tank (8) by Liquid level adjusting valve; And by the unlatching of liquid level controller (32) control Liquid level adjusting valve.
12. methods according to claim 9, is characterized in that:
Pass through pump (9) by final oil product (21) transmitting system from described oil product collecting tank (8).
13. methods according to claim 9, is characterized in that:
Described gas comprises make-up gas (11), recyclegas (16), and above-mentioned gas is inert gas, is preferably one of nitrogen, helium, argon gas.
14. according to the method one of claim 9 ~ 13 Suo Shu, it is characterized in that:
The interior operating temperature of described regenerated catalyst de-oiling tank (1) is 250 ~ 300 DEG C, and operating pressure is 0.7 ~ 0.8MPa (G), and gas agent volume ratio is 300:1 ~ 800:1;
The interior operating temperature of described gs-oil separator (5) is not higher than 55 DEG C, and operating pressure is 0.4 ~ 0.5MPa (G).
15. methods according to claim 14, is characterized in that:
The interior operating temperature of described gs-oil separator (5) is 40 ~ 55 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310016047.2A CN103920541A (en) | 2013-01-16 | 2013-01-16 | Boiling-bed hydrogenation catalyst de-oiling system and method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310016047.2A CN103920541A (en) | 2013-01-16 | 2013-01-16 | Boiling-bed hydrogenation catalyst de-oiling system and method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103920541A true CN103920541A (en) | 2014-07-16 |
Family
ID=51139074
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310016047.2A Pending CN103920541A (en) | 2013-01-16 | 2013-01-16 | Boiling-bed hydrogenation catalyst de-oiling system and method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103920541A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108328761A (en) * | 2017-08-29 | 2018-07-27 | 华东理工大学 | MTO washes the method and device of hydraulic art continuous operation cycle stretch-out |
| CN109999731A (en) * | 2019-04-26 | 2019-07-12 | 河南百优福生物能源有限公司 | The online charging method of the catalyst of biomass pyrolysis liquid fluidized bed reactor and device |
| CN110624525A (en) * | 2018-06-21 | 2019-12-31 | 中国石化工程建设有限公司 | Active coke regeneration system and method |
| CN113383056A (en) * | 2018-12-18 | 2021-09-10 | Ifp 新能源公司 | Process for hydrodesulphurization of gasoline cuts containing sulphur olefins using regenerated catalyst |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5772901A (en) * | 1996-04-30 | 1998-06-30 | Energy Biosystems Corporation | Oil/water/biocatalyst three phase separation process |
| CN102527448A (en) * | 2011-12-21 | 2012-07-04 | 神华集团有限责任公司 | Catalyst de-oiling method and device |
| CN202447098U (en) * | 2011-12-21 | 2012-09-26 | 神华集团有限责任公司 | Catalyst oil removing device |
| CN102698818A (en) * | 2012-06-21 | 2012-10-03 | 上海华畅环保设备发展有限公司 | Processing method and processing device for graded desorption of residue hydrotreating excretion catalyst in ebullated bed |
-
2013
- 2013-01-16 CN CN201310016047.2A patent/CN103920541A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5772901A (en) * | 1996-04-30 | 1998-06-30 | Energy Biosystems Corporation | Oil/water/biocatalyst three phase separation process |
| CN102527448A (en) * | 2011-12-21 | 2012-07-04 | 神华集团有限责任公司 | Catalyst de-oiling method and device |
| CN202447098U (en) * | 2011-12-21 | 2012-09-26 | 神华集团有限责任公司 | Catalyst oil removing device |
| CN102698818A (en) * | 2012-06-21 | 2012-10-03 | 上海华畅环保设备发展有限公司 | Processing method and processing device for graded desorption of residue hydrotreating excretion catalyst in ebullated bed |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108328761A (en) * | 2017-08-29 | 2018-07-27 | 华东理工大学 | MTO washes the method and device of hydraulic art continuous operation cycle stretch-out |
| CN108328761B (en) * | 2017-08-29 | 2023-08-29 | 华东理工大学 | Method and device for prolonging continuous operation period of MTO water washing process |
| CN110624525A (en) * | 2018-06-21 | 2019-12-31 | 中国石化工程建设有限公司 | Active coke regeneration system and method |
| CN113383056A (en) * | 2018-12-18 | 2021-09-10 | Ifp 新能源公司 | Process for hydrodesulphurization of gasoline cuts containing sulphur olefins using regenerated catalyst |
| CN109999731A (en) * | 2019-04-26 | 2019-07-12 | 河南百优福生物能源有限公司 | The online charging method of the catalyst of biomass pyrolysis liquid fluidized bed reactor and device |
| CN109999731B (en) * | 2019-04-26 | 2022-04-12 | 河南百优福生物能源有限公司 | Online catalyst filling method and device for biomass pyrolysis liquid fluidized bed reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP2018535280A5 (en) | ||
| CN103920541A (en) | Boiling-bed hydrogenation catalyst de-oiling system and method thereof | |
| CN103180416A (en) | Method for producing hydrocarbon oil and system for producing hydrocarbon oil | |
| CN205368255U (en) | Semicontinuous device of mink cell focus lightization in overcritical solvent environment | |
| CN102115678B (en) | Hydrogenation and desulfurization method of diesel oil and device thereof | |
| CN202447098U (en) | Catalyst oil removing device | |
| WO2017123262A1 (en) | Quenching vacuum distillation column wash zone liquid | |
| CN104945211B (en) | Heat extraction and catalyst circulation method in catalytic reaction for preparing hydrocarbons from methanol | |
| CN103691211A (en) | Rotational-flow purifying device for gaseous product in fluidized-bed residual oil hydrogenation reactor and method for purifying gaseous product by same | |
| CN105670707A (en) | Automatic cycle device and method for gas washing water (ammonia water) | |
| CN102527448A (en) | Catalyst de-oiling method and device | |
| WO2007040401A1 (en) | Method and plant for preprocessing crude methanol having a paraffin content | |
| CN102115679B (en) | Method and device for producing low-sulfur diesel | |
| CN104086346B (en) | A kind of energy reclaiming method of oxygenatedchemicals propylene technique | |
| CN203744755U (en) | Condenser | |
| CN211329301U (en) | Online sampling and separating device for high-temperature multiphase flow | |
| CN105985804B (en) | A kind of mink cell focus processing technology and processing unit (plant) | |
| CN102041041B (en) | Rotational-flow liquid removal method and device of liquid phase circulation hydrogenation system | |
| CN204298335U (en) | Catalyst transport equipment and the medium-sized reaction unit of catalytic cracking | |
| CN103789011B (en) | A kind of wax hydrofining post-treating method | |
| CN210021399U (en) | Methanol filtering device and system for removing wax of methanol system | |
| CN103611329B (en) | Method and device for reducing rich liquid regeneration energy consumption by adopting spraying flashing-cyclone degassing and coupling process | |
| CN102319523B (en) | Mini-hydrocyclone solid removing method and device for medium oil in fractionating tower of ethylene unit | |
| CN102228843B (en) | Degassing method for degassing tank of catalytic pyrolysis apparatus | |
| CN102218232B (en) | Oil-water separation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20140716 |