CN100387328C - Catalyst particle reverse pressure transfer method and its device - Google Patents
Catalyst particle reverse pressure transfer method and its device Download PDFInfo
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- CN100387328C CN100387328C CNB2005100596275A CN200510059627A CN100387328C CN 100387328 C CN100387328 C CN 100387328C CN B2005100596275 A CNB2005100596275 A CN B2005100596275A CN 200510059627 A CN200510059627 A CN 200510059627A CN 100387328 C CN100387328 C CN 100387328C
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Abstract
The present invention relates to a method and a device for transferring catalyst particles in a reverse pressure way, which belongs to a method and a device for transferring solid particles. In order to solve the problems of strict technical requirements on a catalyst trip valve in the process of transferring the present solid catalyst particles, and much dust of catalyst, a transmitting method which comprises the steps of decompression, charging, pressurization and discharging is provided. Moreover, the existing device is improved, and a device of which the diameter is reduced is added and is combined with a method that pressurization is first carried out and cutting is then carried out, so a catalyst trip valve is omitted and the abrasion of catalyst is decreased.
Description
Technical field
The present invention relates to a kind of carrying method and device of solid particle, more particularly, the present invention relates to a kind of solid catalyst particle is transported to method and device thereof the permanent high-pressure bottle from permanent low pressure vessel.
Background technology
In industry, need sometimes solid particle is transported to a permanent high-pressure bottle from a permanent low pressure vessel, for example need catalyst with inactivation to be transported to the higher regenerator of pressure in the naphtha CONTINUOUS REFORMER process and regenerate from the reactor that is in low pressure.
France Inst Francais Du Petrole a kind of by using the mobile machine parts contact with particle that particle is transported to the method and apparatus of high reduction section from the low pressure epimere is and the immediate prior art of the present invention.Described device comprises low pressure upper container, transformation middle part container, high pressure bottom container, the device to middle part container air feed, the device of a middle part container venting.The following transfer of granules conduit that is communicated with last transfer of granules conduit, connection middle part container and the bottom container of upper container and middle part container, be connected in the last wireway between upper container and the middle part container and go up balanced valve, be connected in the catalyst transport between upper container and the middle part container and go up catalyst stop valve, airtight valve, the downtake that is connected between middle part container and the bottom container reaches balanced valve down, the catalyst transport that is connected between middle part container and the bottom container reaches catalyst stop valve, airtight valve down, and control device.Realize being linked in sequence between above-mentioned three sections respectively.The variation of transformation middle part container pressure is by upper and lower wireway and subsidiary upper and lower balanced valve thereof, feeder, means of deflation, and the co-operating of catalyst stop valve, airtight valve realizes.Instantly balanced valve cuts out, catalyst stop valve, airtight valve are closed down; When making middle part container pressure and upper container pressure approximately equal by means of deflation, last balanced valve is slowly opened, the middle part container pressure drops to the low pressure upper container and equates, last catalyst stop valve, airtight valve are opened, catalyst granules enters the middle part container from the low pressure upper container, and the particle flow in the middle part of this moment between container and the high pressure bottom container is closed by following catalyst stop valve and ended; After the middle part container is filled particle, last catalyst stop valve at first cuts out, going up airtight valve then closes, last balanced valve cuts out, boost for the middle part container by making-up air device, during to middle part container pressure and bottom container pressure approximately equal, following balanced valve is slowly opened, the middle part container pressure rises to the high pressure bottom container and equates, following catalyst stop valve, airtight valve is opened, and catalyst granules enters the high pressure bottom container from the middle part container, when catalyst material level in the container of middle part reaches low material level, close down the catalyst stop valve, close down the catalyst airtight valve then, following balanced valve.The weak point of this method is: when the catalyst stop valve cut out, the intensity and the material that directly contact valve with catalyst required very high; Serious to catalyst abrasion simultaneously, increased the catalyst powder dust quantity, increased the radially possibility of bed obstruction of upstream device.
Summary of the invention
The objective of the invention is on the basis of the existing method that solid catalyst particle is transported to the high pressure bottom container from the low pressure upper container, provide a kind of solid catalyst particle course of conveying that the specification requirement of catalyst stop valve is reduced, and the method and apparatus that catalyst dust reduces.
The present invention is transported to the next container from upper container through intermediate receptacle with solid particle, and the pressure of the next container is higher than the pressure of upper container, and concrete technical scheme is as follows.
Catalyst particle reverse pressure transfer method of the present invention may further comprise the steps:
(1) step-down: close the following balanced valve that connects intermediate receptacle and the next container, close the airtight valve between intermediate receptacle and the next container, opening means of deflation to upper container equates substantially with intermediate receptacle pressure, close means of deflation, open the last balanced valve that connects upper container and intermediate receptacle, connect the last wireway between upper container and the intermediate receptacle, the pressure of intermediate receptacle is equated with the pressure of upper container;
(2) charging: when upper container reaches high charge level, open the airtight valve between upper container and the intermediate receptacle, make the particle in the upper container enter intermediate receptacle through last particle transport pipe, intermediate receptacle begins charging, when intermediate receptacle reaches high charge level, close and close balanced valve, change the pressure period over to;
(3) pressurization: open making-up air device, boost, during to intermediate receptacle pressure and bottom container pressure approximately equal, close making-up air device to intermediate receptacle; This moment, catalyst granules stopped to flow, closed the airtight valve between upper container and the intermediate receptacle, opened down balanced valve, connected the downtake between intermediate receptacle and the next container, and the pressure of intermediate receptacle is equated with the pressure of the next container;
(4) discharging: open the airtight valve between intermediate receptacle and the next container, make the particle in the intermediate receptacle enter the next container through following particle transport pipe.
After above-mentioned discharging step, can also have one and keep step, the state after the maintenance discharging step to regulate particle transport speed, keeps entering depressurization step after the step, forms a continuous conveying process.
In carrying method of the present invention, the pressure differential of preferred upper container and the next container is 0.05-0.7MPa.
In carrying method of the present invention, the size of preferred catalyst particle is 0.5-5mm.
Realize the device of catalyst reverse pressure transfer method of the present invention, comprise upper container 1, intermediate receptacle 2 and the next container 3 and go up particle transport pipe 8, down particle transport pipe 11, means of deflation, making-up air device, go up wireway 4, downtake 6, undergauge device 9, go up airtight valve 10, down airtight valve 12, go up balanced valve 5, balanced valve 7 down;
Described intermediate receptacle 2 be positioned under the upper container 1 and the next container 3 on; Described go up particle transport pipe 8 be positioned under the upper container 1 and intermediate receptacle 2 on, upper container 1 and intermediate receptacle 2 are communicated with, particle transport pipe is provided with airtight valve 10 on this; Described down particle transport pipe 11 be positioned under the intermediate receptacle 2 and the next container 3 on, will be under the intermediate receptacle 2 and the next container 3 be communicated with, this time particle transport pipe is provided with down airtight valve 12; Described means of deflation is the pipeline that connects between intermediate receptacle 2 and the atmosphere, and control valve 13 is housed on it; Described making-up air device is to connect inert gas in the pipeline of intermediate receptacle, and its inlet connects inert gas, and gas pressure is higher than the next container pressure, and outlet is connected in intermediate receptacle top, and control valve 14 is housed on the pipeline; Described going up on the wireway 8 is equipped with balanced valve 5, and wireway links to each other with intermediate receptacle 2 with upper container 1 on this; On the described downtake 6 balanced valve 7 is housed down, this downtake links to each other with the next container 3 with intermediate receptacle 2; Described undergauge device 9 is positioned on the particle transport pipe 8, and above last airtight valve 10.
Described upward particle transport pipe 8 and following particle transport pipe 11 general vertical installations also can tilt to install, but should spend less than 40 with the angle of vertical direction.Should determine the length of this section carrier pipe according to system's pressure reduction, the length homologous ray pressure reduction of this section carrier pipe roughly is directly proportional, and its proportionality coefficient abbreviates length factor as.The length factor scope is generally in 3000mm/MPa～30, between the 000mm/MPa.
Described undergauge device 9 is preferably the undergauge orifice plate, and its diameter is preferably 0.3～0.7 times of particle transport pipe 8 diameters.
The main distinction of the present invention and background technology is to have removed original two catalyst stop valves, has increased a undergauge device, afterwards closes the control mode of valve in conjunction with pressurizeing earlier, has realized carrying method of the present invention.The catalyst stop valve is another foreign patent technology, and manufacturing technology requires high, and difficulty is big, and the cost height is introduced 20,000 dollars of deck valve Men Yuexu.Because the particularity and the importance of valve, these two valves all leave service valve respectively, in order to changing at any time, so once need buy 4.Owing to directly contact with catalyst when closing valve, valve uses a period of time (being about 1 year) just to need to change, and has increased operating cost.In addition, some catalyst are ground when valve closing, have increased the loss of catalyst, particularly Po Sui catalyst enters the equipment (for example regenerator of CONTINUOUS REFORMER) of back, causes Johnson to net obstruction easily, has a strong impact on ordinary production, even stop work and handle, cause bigger loss.By increasing a undergauge device, change control mode and realized of the termination of upper container to the intermediate receptacle catalyst transport.In pressure process, the beginning catalyst flows from top to bottom at last particle transport pipe, when reaching the requirement material level, making-up air device is to intermediate receptacle make-up gas rising pressure, and during high 0.03 MPa of the upper container of intermediate receptacle pressure ratio, catalyst stops to flow, be full of catalyst more than the undergauge device this moment, the undergauge device closes subsequently and closes airtight valve with the underground pipelines gassy, does not contact with catalyst when airtight valve is closed in the assurance.Catalyst granules depends primarily on the internal diameter of undergauge device from the discharge rate of undergauge device, and in addition, blanking speed is also relevant with structure, structure of container and the wall roughness of particle diameter, angle of repose, undergauge device.The undergauge device is a key point of the present invention, and it has not only substituted the catalyst stop valve, has saved investment and operating cost, still influences the key factor of catalyst granules conveying capacity.The present invention has reduced catalyst abrasion owing to cancelled the catalyst stop valve, guarantees the long-term operation of back equipment, has good economic benefit.
The present invention is to provide method and the device of catalyst granules from upper container transport to the next container, the termination that catalyst granules flows between upper container and the intermediate receptacle is to realize by the pressure reduction between upper and lower two containers, in the container pressure uphill process of middle part, last particle transport pipe inner catalyst stops to flow, be full of catalyst granules more than the undergauge device, the undergauge device is blank pipe with the underground pipelines, closes then and closes airtight valve.Do not contact during valve closing with catalyst granules.The termination that catalyst granules flows between intermediate receptacle and the bottom container is till dependence gravity is put only naturally, and this is the interior catalyst-free particle of particle transport pipe at present, does not contact with catalyst granules during valve closing.This is the essential distinction of the present invention and prior art, and it has alleviated the severity that the valve material is required greatly, and to the wearing and tearing of catalyst granules.Thereby the present invention does not have any requirement to the catalyst stop valve, can replace with common valve, can cancel this valve yet, and airtight valve is not had excessive demand.The present invention does not need special catalyst stop valve, has reduced plant investment and operating cost.
Description of drawings
Fig. 1 is a kind of schematic representation of apparatus that realizes the inventive method.
The specific embodiment
The present invention is described in further detail below in conjunction with drawings and Examples.
Below in conjunction with Fig. 1 in detail catalyst granules carrying method of the present invention is described in detail.
Realization shown in Figure 1 particle transport device of the present invention comprises a upper container 1, an intermediate receptacle 2 and a bottom container 3, intermediate receptacle 2 be positioned under the upper container 1 and bottom container 3 on.Last particle transport pipe 8 be positioned under the upper container 1 and intermediate receptacle 2 on, both are communicated with.Following particle transport pipe 11 be positioned under the intermediate receptacle 2 and bottom container 3 on, both are communicated with.The two ends of last wireway 4 are connected to upper container 1 and intermediate receptacle 2, and balanced valve 5 is housed on it; The two ends of downtake 6 are connected to intermediate receptacle 2 and bottom container 3, and balanced valve 7 is housed down on it.By control means of deflation 13, making-up air device 14, go up airtight valve 10, airtight valve 12 and go up the opening and closing state of balanced valve 5 and following balanced valve 7 down, can make pressure conversion between high pressure and low pressure of intermediate receptacle 2.In particle transport device shown in Figure 1, the middle part of last particle transport pipe 8 is provided with undergauge orifice plate 9.The diameter of undergauge orifice plate 9 is 0.3～0.7 times of last particle transport pipe 8 diameters.
Among Fig. 1, that section between intermediate receptacle 2 and the upper container 1 gone up the 8 general vertical installations of particle transport pipe, also can tilt to install, but should spend less than 40 with the angle of vertical direction.Should determine the length of this section carrier pipe according to system's pressure reduction.The length homologous ray pressure reduction of this section carrier pipe roughly is directly proportional, and its proportionality coefficient abbreviates length factor as.The length factor scope is generally in 3000mm/MPa～30, between the 000mm/MPa.This coefficient has relation with the diameter ratio of upper container 1 and this section carrier pipe, and promptly length factor is big more, and the above-mentioned diameter ratio that is allowed can be more little.Generally speaking, system's pressure reduction increases 0.1MPa, and pipe range increases 500mm, and allow above-mentioned diameter ratio to may diminish to 5 this moment.
Following particle transport pipe 11 between intermediate receptacle 2 and the next container 3, its structure and installation requirement are identical with last particle transport pipe 8.
According to the requirement of external system, upper container 1 and the next container 3 need remain on a pressure stable state respectively, and the pressure perseverance of upper container 1 is lower than the pressure of the next container 3, and the difference of two pressure is called system's pressure reduction.As a special case, in the course of conveying of PETROLEUM PROCESSING catalytic reforming beaded catalyst, generally between 0.16～1.6MPa, generally between 0.2～1.7MPa, system's pressure reduction generally remains between 0.05～0.7MPa the pressure limit of the next container 3 pressure limit of upper container 1.
The particle that the present invention is suitable for carrying, granular size is generally 0.5～5mm.
Pre-install material before the conveying solid substance particle earlier, make upper container 1 and intermediate receptacle 2 be in high charge level and low material level respectively.The steady low-pressure gas of upper container 1 connection system, bottom container 3 is communicated with the stable high-pressure gas systems.
Particle transport process of the present invention comprises following four steps: step-down, charging, pressurization, discharging.
(a) step-down: close down balanced valve 7, close the following airtight valve 12 between intermediate receptacle 2 and the next container 3, balanced valve 5 is closed in the pass, close the last airtight valve 10 between intermediate receptacle 2 and the upper container 1, open means of deflation 13, be depressured to upper container 1 and equate substantially with intermediate receptacle 2 pressure, close means of deflation 13, open balanced valve 5, connect the last wireway 4 between upper container 1 and the intermediate receptacle 2, the pressure of intermediate receptacle 2 is equated with the pressure of upper container 1;
(b) charging: wait for when upper container 1 reaches high charge level, open the last airtight valve 10 between upper container 1 and the middle part container 2, middle part container 2 begins charging.When middle part container 2 reaches high charge level, close and close balanced valve 5, change the pressure period over to.
(c) pressurization: open making-up air device 14, boost for intermediate receptacle 2, during to middle part container 2 pressure and the next container 3 pressure approximately equals, close making-up air device 14.This moment, catalyst granules stopped to flow, and the reducing orifice plate is full of catalyst more than 9, and reducing orifice plate 9 following emptying catalyst are blank pipe, close the last airtight valve 10 between upper container 1 and the intermediate receptacle 2.Open down balanced valve 7, connect the downtake 6 between intermediate receptacle 2 and the next container 3, the pressure of intermediate receptacle 2 is equated with the pressure of bottom container 3; Change the discharging stage over to.
(d) discharging: open the following airtight valve 12 between intermediate receptacle 2 and the bottom container 3, make the particle in the intermediate receptacle 2 enter the next container 3 through following particle transport pipe 11, after the catalyst granules emptying in the middle container 2, be blank pipe in the following particle transport pipe 11, go to buck stage.
Circulate continuously as the particle transport step 1 of the present invention and carry out.For example, if there is the particle in the low pressure external container (the upper container 1 of its pressure ratio is slightly high or identical) constantly to be joined upper container 1, make the material level of upper container 1 keep being not less than the low material level of setting, simultaneously the particle in the next container 3 constantly is transplanted on a high voltage external container (its pressure ratio the next container 3 lower slightly or identical), make the material level of the next container 3 keep not being higher than the high charge level of setting, there are enough space assurance discharging steps to carry out smoothly, then after step (d) finishes, promptly restart the operation of step (a), just carry particle serially.
Used voltage stabilizing gas should follow the low pressure external container that links to each other with the present invention identical with the gas medium in the high voltage external container with the kind of carrying gas, perhaps is inertia and does not pollute to be transferred particle for the gas medium in low pressure external container that links to each other with the present invention and the high voltage external container.
Continuously during cycling, step (d) can have a maintenance process after finishing.State when this process keeps step (d) to finish only is the beginning of waiting for down-circulating, and is used to regulate the transfer rate of particle.Restart the operation of step (a) after the maintenance process finishes, carry out next circulation.Obviously, when this process time is zero, only carry out the circulation of step (a) to (d), device is carried particle at full capacity.
But the opening and closing manual operation of each valve is carried out in the particle transport process of the present invention, a control system also can be installed certainly be controlled.Because the termination of particle flow of the present invention is easy to control, therefore only need simple classical control system to get final product.This point is described in invention effect part.
Particle transport method of the present invention and device thereof, can be widely used in need be with solid particle from the industrial process of low pressure vessel to the high-pressure bottle conveying, as the catalyst granules course of conveying in oil and the Chemical Manufacture.
Be the exemplary embodiments that the present invention is applied to naphtha CONTINUOUS REFORMER process below.Contrast Fig. 1 is illustrated.
The reforming reaction process generates with coke.Along with the increase of reforming catalyst area carbon, the necessary coke burning regeneration of catalyst uses catalyst circulation.Reclaimable catalyst is sent into reactor after regenerating in regenerator.Catalyst after the regeneration is in the regenerator, regenerator pressure 0.56MPa, reactor bottom pressure 0.32MPa, connecting portion's container 1 pressure is 0.29MPa, be lower than regenerator pressure, catalyst transport between from the reactor bottom to regenerator the present invention just can solve.
Reacted reforming catalyst particle rises to upper container 1 from the most last reactor bottom (not shown), and is accumulated in upper container 1 bottom.The pressure ratio of upper container 1 about the low 30kPa of pressure of last reactor bottom, is 0.29MPa.
Intermediate receptacle 2 (locking hopper) is equipped with level-sensing device, monitoring material level, pressure monitoring instrument, monitoring pressure.
The storing section that the next container 3 is regenerators, pressure are 0.56MPa.
Last particle transport pipe 8 diameters (internal diameter) are 80mm, length 1500mm; The diameter of undergauge orifice plate 9 is 45mm, and its diameter increases the blanking amount and increases.
Making-up air device is a pipeline that links to each other with nitrogen pot, and diameter is 80mm, and controllable valve is housed on it, connects the 1.25MPa source nitrogen.
Means of deflation is a pipeline that links to each other with atmosphere, and diameter is 50mm, and controllable valve is housed on it.
The nominal diameter of last wireway 4 and downtake 6 and last balanced valve 5 and following balanced valve 7 all is 40mm.
The operating process circulation step is as follows:
(a) step-down: close down balanced valve 7, close the following airtight valve 12 between intermediate receptacle 2 and the next container 3, balanced valve 5 is closed in the pass, close the last airtight valve 10 between intermediate receptacle 2 and the upper container 1, open vent valve 13, be depressured to intermediate receptacle 2 and equate (pressure reduction is less than 0.05MPa) substantially with upper container 1 pressure, close vent valve 13, open balanced valve 5, connect the last wireway 4 between upper container 1 and the intermediate receptacle 2, the pressure of intermediate receptacle 2 is reduced to the pressure of upper container 1 equate;
(b) charging: wait for when upper container 1 reaches the high charge level of appointment (65%), open the last airtight valve 5 between upper container 1 and the intermediate receptacle 2, intermediate receptacle 2 begins charging.High charge level occurs in the intermediate receptacle 2, and catalyst is full of.Last balanced valve 5 cuts out, and changes the pressure period over to.
(c) pressurization: open making-up air device 14, nitrogen boosts for intermediate receptacle 2, during to intermediate receptacle 2 pressure and the next container 3 pressure approximately equals (pressure reduction is less than 0.05MPa), closes making-up air device 14.This moment, catalyst granules stopped to flow, and the reducing orifice plate is full of catalyst more than 9, and reducing orifice plate 9 following emptying catalyst are blank pipe, close the last airtight valve 10 between upper container 1 and the intermediate receptacle 2.Open down balanced valve 7, connect the downtake 6 between intermediate receptacle 2 and the next container 3, the pressure of intermediate receptacle 2 is risen to the pressure of the next container 3 equate; Change the discharging stage over to.
(d) discharging: open the following airtight valve 12 between intermediate receptacle 2 and the next container 3, make the catalyst granules in the intermediate receptacle 2 enter the next container 3 through following particle transport pipe 11, after the catalyst granules emptying in the middle container 2, be blank pipe in the following particle transport pipe 11, go to buck stage.
Keep: this process waits for that without any action upper container reaches the appointment material level.
Whole circulation is lasted 45 minutes.Operating point is positioned at 90% point of device load.
Claims (7)
1. catalyst particle reverse pressure transfer method is characterized in that it may further comprise the steps:
(1) step-down: close the following balanced valve that connects intermediate receptacle and the next container, close the airtight valve between intermediate receptacle and the next container, opening means of deflation to upper container equates substantially with intermediate receptacle pressure, close means of deflation, open the last balanced valve that connects upper container and intermediate receptacle, connect the last wireway between upper container and the intermediate receptacle, the pressure of intermediate receptacle is equated with the pressure of upper container;
(2) charging: when upper container reaches high charge level, open the airtight valve between upper container and the intermediate receptacle, make the particle in the upper container enter intermediate receptacle through last particle transport pipe, intermediate receptacle begins charging, when intermediate receptacle reaches high charge level, close and close balanced valve, change the pressure period over to;
(3) pressurization: open making-up air device, boost, during to intermediate receptacle pressure and bottom container pressure approximately equal, close making-up air device to intermediate receptacle; This moment, catalyst granules stopped to flow, closed the airtight valve between upper container and the intermediate receptacle, opened down balanced valve, connected the downtake between intermediate receptacle and the next container, and the pressure of intermediate receptacle is equated with the pressure of the next container;
(4) discharging: open the airtight valve between intermediate receptacle and the next container, make the particle in the intermediate receptacle enter the next container through following particle transport pipe.
2. carrying method as claimed in claim 1 is characterized in that, after described discharging step, have one and keep step, the state after the maintenance discharging step is to regulate particle transport speed, keep entering described depressurization step after the step, form a continuous conveying process.
3. carrying method as claimed in claim 1 or 2 is characterized in that, the pressure differential of described upper container and the next container is 0.05-0.7MPa.
4. carrying method as claimed in claim 1 or 2 is characterized in that, the size of described catalyst granules is 0.5-5mm.
5. device of realizing claim 1,2,3 or 4 described carrying methods, it comprise upper container (1), intermediate receptacle (2) and the next container (3) and go up particle transport pipe (8), down particle transport pipe (11), means of deflation, making-up air device, go up wireway (4), downtake (6), go up airtight valve (10), down airtight valve (12), go up balanced valve (5), balanced valve (7) down; It is characterized in that it also comprises undergauge device (9);
Described intermediate receptacle (2) be positioned under the upper container (1) and the next container (3) on; Described upward particle transport pipe (8) is positioned under the upper container (1) and on the intermediate receptacle (2), upper container (1) and intermediate receptacle (2) is communicated with, and last particle transport pipe is provided with airtight valve (10); Described down particle transport pipe (11) be positioned under the intermediate receptacle (2) and the next container (3) on, with intermediate receptacle (2) and the next container (3) connection, following particle transport pipe is provided with down airtight valve (12); Means of deflation is the pipeline that connects between intermediate receptacle (2) and the atmosphere, and control valve (13) is housed on it; Described making-up air device is to connect the pipeline of inert gas to intermediate receptacle, and its inlet connects inert gas, and gas pressure is higher than the next container pressure, and outlet is connected in intermediate receptacle top, and control valve is housed on the pipeline; Described going up on the wireway (4) is equipped with balanced valve (5), and last wireway (8) links to each other with intermediate receptacle (2) with upper container (1); Balanced valve (7) is housed down on the described downtake (6), and downtake (6) links to each other with the next container (3) with intermediate receptacle (2); Described undergauge device (9) is positioned on the particle transport pipe (8), and in last airtight valve (10) top.
6. device as claimed in claim 5 is characterized in that, describedly goes up particle transport pipe (8) and following particle transport pipe (11) is vertically installed or the installation of tilting; When tilting to install, should spend less than 40 with the angle of vertical direction; The length of described upward particle transport pipe (8) and following particle transport pipe (11) and the ratio of the pressure reduction between upper container and the next container are in 3000mm/MPa～30, between the 000mm/MPa.
7. device as claimed in claim 5 is characterized in that, described undergauge device (9) is the undergauge orifice plate, and its diameter is 0.3～0.7 times of last particle transport pipe (8) diameter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100596275A CN100387328C (en) | 2005-03-29 | 2005-03-29 | Catalyst particle reverse pressure transfer method and its device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100596275A CN100387328C (en) | 2005-03-29 | 2005-03-29 | Catalyst particle reverse pressure transfer method and its device |
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| Publication Number | Publication Date |
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| CN1686603A CN1686603A (en) | 2005-10-26 |
| CN100387328C true CN100387328C (en) | 2008-05-14 |
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| CNB2005100596275A Expired - Fee Related CN100387328C (en) | 2005-03-29 | 2005-03-29 | Catalyst particle reverse pressure transfer method and its device |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102049223B (en) * | 2009-10-27 | 2012-09-12 | 中国石油化工股份有限公司 | Device and method for filling catalyst on line by pneumatic transmission |
| CN108946176A (en) * | 2017-05-19 | 2018-12-07 | 中国石化工程建设有限公司 | A kind of devices and methods therefor of catalyst safe transport between mutual exclusion environment |
| CN108889249A (en) * | 2018-08-09 | 2018-11-27 | 北京拓川科研设备股份有限公司 | A kind of moving bed reaction equipment and feed process |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1059163A (en) * | 1990-08-24 | 1992-03-04 | 上海高桥石化公司炼油厂 | The device of automatic catalyst-feeding and technology |
| CN1139528C (en) * | 1999-05-10 | 2004-02-25 | 中国石化集团洛阳石油化工工程公司 | Method and equipment for transporting solid particles |
-
2005
- 2005-03-29 CN CNB2005100596275A patent/CN100387328C/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1059163A (en) * | 1990-08-24 | 1992-03-04 | 上海高桥石化公司炼油厂 | The device of automatic catalyst-feeding and technology |
| CN1139528C (en) * | 1999-05-10 | 2004-02-25 | 中国石化集团洛阳石油化工工程公司 | Method and equipment for transporting solid particles |
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| CN1686603A (en) | 2005-10-26 |
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