CN207933355U - Boiling bed hydrogenation consersion unit - Google Patents
Boiling bed hydrogenation consersion unit Download PDFInfo
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- CN207933355U CN207933355U CN201820188358.5U CN201820188358U CN207933355U CN 207933355 U CN207933355 U CN 207933355U CN 201820188358 U CN201820188358 U CN 201820188358U CN 207933355 U CN207933355 U CN 207933355U
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- bed hydrogenation
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Abstract
The utility model belongs to hydrogen addition technology field, and in particular to a kind of boiling bed hydrogenation consersion unit.The boiling bed hydrogenation consersion unit, system is added including boiling bed hydrogenation reactor, catalyst and adds agent pipeline, wherein, it includes catalyst storage tank and the catalyst delivery line for being connected to catalyst storage tank and boiling bed hydrogenation reactor inner space that system, which is added, in catalyst, at least two valves are set on catalyst delivery line, catalyst delivery line between two valves and add pipeline connection is revealed using anti-hydrogen sulfide between agent pipeline, at least one valve is set on anti-hydrogen sulfide leakage pipeline.Boiling bed hydrogenation consersion unit described in the utility model solves catalyst and the system security risk that interior leakage is brought caused by frequent operation under special operation condition is added；The utilization rate for further improving reactor improves hydrogenation reaction effect, improves the stability of device operation.
Description
Technical field
The utility model belongs to hydrogen addition technology field, and in particular to a kind of boiling bed hydrogenation consersion unit.
Background technology
Boiling bed hydrogenation reaction refers to feedstock oil (predominantly liquid phase), hydrogen (gas phase) carries out adding hydrogen on catalyst (solid phase)
The process of reaction, hydrogenation reaction mainly occur hydrodesulfurization, hydrodenitrogeneration, hydrogenation deoxidation plus hydrogen and are saturated, are hydrocracked.Instead
Device is answered to be operated under the fluidized state of gas, liquid, solid three-phase, catalyst is in the feedstock oil entered from reactor bottom and the band of hydrogen
Under dynamic, it is in fluidized state, entirely different fluid state is in fixed bed reactors.Boiling bed hydrogenation reaction can be handled
The inferior feedstock oil of high metal, high asphalt content, reaction is small with pressure drop, temperature is uniform, can add row's catalyst online
The features such as to keep catalyst activity.
Boiling bed hydrogenation reactor will generally be arranged catalyst and add heat-extraction system online, be used for the addition and discharge of catalyst.
But catalyst adds heat-extraction system to be not continuous use online, and catalyst updating is carried out when usually reactivity worth does not reach requirement,
According to feedstock property and conversion level requirement, general one week or longer time progress catalyst updating it is primary.System is added in catalyst
For system between normal pressure and the high pressure (General reactions pressure is in 15MPa or more) of reactor, when enabling, opens related each valve, will
Solid material is added along transfer pipeline and relevant device in reactor, again closes related valve after addition.Due to catalysis
Agent addition system operatio is frequent, abrasion of the solid material to valve in addition so that the valves leakage phenomenon of system is added in catalyst
Than other positions valve seriously much.Connect with atmospheric pressure device (such as catalyst stand-by storage) since system is added in catalyst
It connects, the high-hydrogen sulfide gas in reaction system is easy to enter by the valve of leakage in these in atmospheric pressure device or further leakage
To environment, hydrogen sulfide is extremely toxic substance, therefore, certain security risk is brought to safety in production.Currently without suitable solution party
Case can only solve the problems, such as this from the durability of valve, or replace the interior valve leaked in time, increase device operating cost.
Presently, there are two kinds of major type of boiling hydrogen addition technologies, one kind is such as USRe25 by the way of oil phase cycle,
Boiling bed process described in 770, the deficiency of this technique in practical applications are：To keep solid-liquor separation effect, reactor
Interior catalyst amount cannot be too many, and reactor utilization rate is low, industrial fluidized bed reactor utilization rate generally only 40% or so (profit
Refer generally to the percentage that loaded catalyst accounts for reactor volume (disregarding end socket space), fixed bed reactors utilization rate one with rate
As 90% or more)；Reactor has larger space to keep residence time of the liquid material under no catalytic condition long, this position
There is no hydrogenation reaction, material to be easy reaction coking at high temperature.Another kind of is that three phase separator is arranged in reactor, is being reacted
Device internal upper part carries out gas-liquid-solid separation, such as the fluidized bed reactor that CN 02109404.7 is introduced, passes through in setting by the program
Three phase separator is set, the dosage of catalyst can be improved, that is, that improves reactor utilizes space, but in actual use, catalysis
Agent dosage raising limits, if catalyst amount increases, the separating effect rapid decrease of three phase separator actually compares the first kind
Fluidized bed reactor utilization rate improves limited；Above-mentioned technology is further improved in CN 200710012680.9, in three-phase
Separator lower part setting guide frame increases the operating flexibility of three phase separator, it is ensured that three phase separator using guide frame
It efficiently separates, reduces the drag-out of catalyst, improve catalyst inventory, improve reactor utilization rate, but when in use, still need to
(as shown in its attached drawing, the region catalytic amount is seldom, does not send out substantially for the certain area's setting catalyst lean phase region in three phase separator lower part
Raw hydrogenation reaction), otherwise the separating effect of three phase separator cannot still be met the requirements, and the presence of dilute-phase zone, influence reactor
The further promotion of utilization rate is (although point out that the catalyst loading in reactor shell can be reactor volume in its specification
40~70%, but it is general also only can be with steady running in the case of 50% or so), also influence hydrogenation reaction effect, and
And after the amplification of reactor scale, catalyst loading is more difficult to improve, it is difficult to achieve the effect that experimental provision.Although the latter is theoretically
Be not required to recycle oil, but go into operation, stop work, operation exception when catalyst can be caused to be difficult to reach stable fluidized state, operation is steady
Qualitative deficiency.Therefore, the utilization ratio of boiling bed hydrogenation reactor how is improved, reaction effect is improved, improves the stabilization of device
Property, it is this field technical issues that need to address.
Utility model content
According to the above-mentioned deficiencies in the prior art, the technical problems to be solved in the utility model is：A kind of ebullated bed is provided
Hydrogenation reaction equipment solves catalyst and the system security risk that interior leakage is brought caused by frequent operation under special operation condition is added；Into
One step improves the utilization rate of reactor, promotes hydrogenation reaction effect, improves the stability of device operation.
System is added in boiling bed hydrogenation consersion unit described in the utility model, including boiling bed hydrogenation reactor, catalyst
System and add agent pipeline, wherein catalyst be added system include catalyst storage tank and be connected to catalyst storage tank and boiling bed hydrogenation it is anti-
The catalyst delivery line of device inner space is answered, at least two valves are set on catalyst delivery line, between two valves
Catalyst delivery line and add pipeline connection revealed using anti-hydrogen sulfide between agent pipeline, be arranged on anti-hydrogen sulfide leakage pipeline to
A few valve.
Described plus agent pipeline is make-up hydrogen compressor outlet line or raw oil pump outlet line.
The boiling bed hydrogenation reactor includes shell and the three phase separator positioned at shell internal upper part, three phase separator
Including two different concentric drums of internal diameter, i.e. inner barrel and outer barrel, the upper and lower ends of inner barrel and outer barrel are all open, outer barrel it is upper
End opening is less than the upper end opening of inner cylinder, and the lower ending opening of outer barrel is less than the lower ending opening of inner cylinder, and outer barrel top is direct tube section, outside
Cylinder lower part is a taper type contraction section, the lower ending opening of lower ending opening, that is, outer barrel of contraction section, the lower ending opening and outer barrel of inner cylinder
Gap is provided between contraction section, shell is the cylinder type shell perpendicular to horizontal plane, and shell, inner barrel and outer barrel are concentric set
It sets, outer barrel is fixed on by support construction in inner walls, and inner cylinder is fixed on by support construction on outer tube inner wall, in inner cylinder
Top is provided with liquid discharge tube line, and upper part of the housing is provided with liquid outlet, and liquid discharge tube line is connected with liquid outlet, outer barrel
The lower section of lower ending opening baffle is set, lower part is provided with distribution plate in shell, and case top is provided with gas vent, shell
Bottom is provided with material inlet and catalyst outlet.
The internal diameter of the direct tube section of the outer barrel is 50~90%, preferably the 75~85% of housing inner diameter.
Between the inner cylinder and outer barrel annular space distance be outer barrel corresponding position radius 30~70%, preferably 40~
60%.
The difference in height of the inner cylinder upper end and outer barrel upper end is 10~50%, preferably the 20~40% of outer barrel radius.
Gap between the lower ending opening and outer barrel contraction section of the inner cylinder is the 5~40% of outer barrel direct tube section radius,
Preferably 10~30%.
10~50%, preferably the 15 of a diameter of outer barrel direct tube section diameter of outer barrel contraction section lower ending opening~
35%.
The angle of throat angle of the outer barrel contraction section is 20 °~80 °, preferably 30 °~60 °.
The height of the outer barrel top direct tube section is 0.4~3m, preferably 0.5~1m.
Gas-phase space is arranged in three phase separator top in the boiling bed hydrogenation reactor, and gas-phase space height is reaction
0~20%, preferably the 5~10% of device shell (not including reactor end socket part).
Three phase separator outer barrel shrinks pars infrasegmentalis direct tube section, i.e. outer barrel is arranged from upper in the boiling bed hydrogenation reactor
Direct tube section-contraction section-straight tube segment structure is followed successively by under.
The baffle is the spindle that upper and lower ends are small, broad in the middle, and spindle axial cross section maximum is a diameter of
1~3 times of outer barrel lower ending opening diameter.It is arranged suitable for gap between baffle and three phase separator outer barrel lower port.
The boiling bed hydrogenation reactor is arranged as required to the reaction liquid phase effluent circulatory system, reaction liquid phase outflow
The object circulatory system includes circulating pump, and pump entry pipeline is connected to the liquid phase region of reactor three phase separator, circulating-pump outlet
It is connected to reactor feed mouth by pipeline.
The bottom of reactor shell is equipped with material (liquid charging stock oil and hydrogen) entrance in the utility model, in three phase separation
Liquid discharge tube line is arranged in top inside device inner cylinder, and the liquid that reaction is generated exports reactor.
The fluidized bed reactor is arranged as required to other components, such as system for detecting temperature, pressure detecting system, stream
Body fluidised form detecting system, catalyst distribution condition detecting system, material reallocation system or catalyst add online one in heat-extraction system
Kind is several.Above-mentioned component can be determined by those skilled in the art by the prior art.
The boiling bed hydrogenation reaction system is arranged as required to corollary apparatus, as raw material pump, heat exchanger, heating furnace,
Separator etc..Above-mentioned corollary apparatus can be determined by those skilled in the art by the prior art.
Using the boiling bed hydrogenation method of boiling bed hydrogenation consersion unit described in the utility model, steps are as follows：
(1) raw material preparation：
Reaction raw materials are heavy or inferior feedstock oil, such as decompression residuum, coal tar, liquefied coal coil, asphalt oil sand, shale oil
Deng；Catalyst is solid particle, and particle diameter (in terms of isometric spherical shape) is 0.6~2mm, catalyst using aluminium oxide as carrier,
It is active component at least one of Mo, W, Ni or Co, while related auxiliaries can be added；Catalyst is in reactor interior loading amount
(in terms of stationary state) is the 50~85% of reactor volume, preferably 65~80%, more preferably 72~78%；
(2) hydrogenation reaction：
Hydrogenation reaction pressure is 5~25MPa, and reaction temperature is 200~500 DEG C, hydrogen and feedstock oil standard state lower body
For product than being 300~2000, volume space velocity of the feedstock oil compared with catalyst volume (stationary state) is 0.1~2h-1, in ebullated bed
In hydrogenation reactor carry out hydrogenation reaction to get.
Boiling bed hydrogenation method described in the utility model when carrying out catalyst addition operation, is closed in operation
The valve on anti-hydrogen sulfide leakage pipeline is closed, normal catalyst is carried out and operation is added.After operation is added in catalyst, anti-sulphur
The valve changed on hydrogen leakage pipeline opens a smaller aperture, closes the valve on catalyst delivery line, a small amount of at this time
New hydrogen feedstock oil enters associated pipe.
The utility model is coupled to each other relationship by what setting plus agent pipeline and catalyst were added system, using adding agent pipeline
The condition of a little higher than reactor pressure of pressure, though related valve in leakage, and new hydrogen feedstock oil enter reactor or into
Enter catalyst storage tank, solves security hidden trouble caused by high-concentration hydrogen sulfide leakage in reactor.In fact, in related valves
Door slightly in leakage the case where need not be repaired or replaced, can obviously reduce operating cost.
Show to influence the factor of three phase separator separating effect in fluidized bed reactor by largely furtheing investigate and not only exist
Structure, material system status in three phase separator, also have much relations with earth rotation.Gas, liquid, solid in fluidized bed reactor
Three-phase state, for gas, liquid generally in the state that flows up, solid catalyst is in boiling quick condition.Earth rotation is to upper
Stating material state has certain active force, forms slight cyclonic action, in the larger reactor of industry, due to scale compared with
Greatly, this cyclonic action more shows.As a result, catalyst is more assembled in the region close to reactor wall, reactor diameter
It is more sparse to central area.This effect produces the separating effect of existing three phase separator and significantly affects, that is, works as catalysis
When agent loadings increase, the solid catalyst that three phase separator is separated settles back the increase of the resistance in reactor, by liquid
The chance that material takes reactor out of improves, and reactor is made to take catalytic amount increase out of.To solve the problems, such as this, usually in three-phase separate
From device lower part be arranged catalyst dilute-phase zone, with overcome catalyst sedimentation flow back resistance, but the measure the result is that reactor
Utilization rate reduces, and reaction effect is affected.Before the utility model, those skilled in the art do not recognize influence boiling
The full content for rising three phase separator separating effect influence factor in a reactor, into without proposing suitable solution.
The utility model is on the basis of the studies above, for earth rotation to flow state in large-scale fluidized bed reactor
Influence, redesigned novel ebullated bed three phase separator, solved problem of the prior art, further increase reactor
Utilization rate (improve catalyst in reactor reserve).
Compared with prior art, the beneficial effects of the utility model are as follows：
1, the solid catalyst that three phase separator separates is flowed back into reaction in reactor radial center regional subsidence
In device, when solving high catalyst loadings, the big problem of resistance of catalyst sedimentation reflux ensure that three phase separator is urged in height
Still there is good separating effect when agent loadings.
2, loaded catalyst ratio, the especially catalyst of large-scale industry fluidized bed reactor can be further increased
Filling ratio.While improving reactor volume utilization rate, catalyst lean phase region is reduced or eliminated, hydrogenation reaction is improved
Effect.
3, the problem of influencing reaction effect caused by overcoming catalyst distribution unevenness caused by earth rotation.The prior art
In, do not consider that the eddy flow of earth rotation influences, catalyst is unevenly distributed to a certain extent, and existing three phase separator will detach
The catalyst sedimentation got off to reactor wall region, exacerbate it is this be unevenly distributed, influencing three phase separator separating effect
While, reaction effect is also influenced, the utility model method solves the deficiency.
4, it solves catalyst and the system security risk that interior leakage is brought caused by frequent operation under special operation condition is added.
Description of the drawings
Fig. 1 is the structural schematic diagram of the utility model；
In figure：1, add agent pipeline；2, catalyst storage tank；3, catalyst delivery line；4, valve；5, anti-hydrogen sulfide leakage pipe
Road；6, shell；7, inner cylinder；8, outer barrel；9, liquid discharge tube line；10, liquid outlet；11, baffle；12, distribution plate；13, gas
Body exports；14, material inlet；15, catalyst outlet.
Specific implementation mode
The embodiments of the present invention are described further below in conjunction with the accompanying drawings：
As shown in Figure 1, boiling bed hydrogenation consersion unit described in the utility model, including boiling bed hydrogenation reactor, urge
Agent be added system and plus agent pipeline 1, wherein catalyst be added system include catalyst storage tank 2 and connection catalyst storage tank 2 and
At least two valves 4 are arranged on catalyst delivery line 3 in the catalyst delivery line 3 of boiling bed hydrogenation reactor inner space,
Catalyst delivery line 3 between two valves 4 with plus agent pipeline 1 between be connected to using anti-hydrogen sulfide leakage pipeline 5, anti-vulcanization
At least one valve 4 is set on hydrogen leakage pipeline 5.Described plus agent pipeline 1 is make-up hydrogen compressor outlet line or raw oil pump
Outlet line.The boiling bed hydrogenation reactor includes shell 6 and the three phase separator positioned at 6 internal upper part of shell, three-phase separate
Include two different concentric drums of internal diameter, i.e. inner cylinder 7 and outer barrel 8 from device, the upper and lower ends of inner cylinder 7 and outer barrel 8 are all open,
The upper end opening of outer barrel 8 is less than the upper end opening of inner cylinder 7, and the lower ending opening of outer barrel 8 is less than the lower ending opening of inner cylinder 7, on outer barrel 8
Portion is direct tube section, and 8 lower part of outer barrel is a taper type contraction section, the lower ending opening of lower ending opening, that is, outer barrel 8 of contraction section, inner cylinder 7
8 contraction section of lower ending opening and outer barrel between be provided with gap, shell 6 is the cylinder type shell 6 perpendicular to horizontal plane, shell 6,
Inner cylinder 7 and outer barrel 8 are concentric setting, and outer barrel 8 is fixed on by support construction on 6 inner wall of shell, and inner cylinder 7 passes through support construction
It being fixed on 8 inner wall of outer barrel, the top in inner cylinder 7 is provided with liquid discharge tube line 9, and 6 top of shell is provided with liquid outlet 10,
Liquid discharge tube line 9 is connected with liquid outlet 10, and baffle 11 is arranged in the lower section of the lower ending opening of outer barrel 8, and lower part is set in shell 6
It is equipped with distribution plate 12,6 top of shell is provided with gas vent 13, and 6 bottom of shell is provided with material inlet 14 and catalyst discharge
Mouth 15.
When system not enabled is added in catalyst, catalyst is simulated by the way of opening very little aperture, system valve is added
Interior leakage operating mode.Make-up hydrogen compressor outlet is passed through with the valve opening on the connecting pipeline of catalyst addition system compared with small guide vane
Hydrogen sulfide is not detected in 24 hours simulated operations, catalyst storage tank and device ambient enviroment.Without using the utility model side
Method, catalyst storage tank is interior to detect higher concentration hydrogen sulfide at once.Illustrate that the utility model has preferable technique effect.
Three phase separator separating effect carries out simulated experiment using chill.The size of cold model unit is：Reactor shell
The outer barrel top of internal diameter 200mm, the height 3500mm of reactor shell, the height 400mm of three phase separator, three phase separator are straight
The diameter 300mm of cylinder section, the annular space distance between inner cylinder and outer barrel is 80mm, and inner cylinder upper end and the difference in height of outer barrel upper end are
60mm, gap between the lower ending opening and outer barrel contraction section of inner cylinder are 60mm, a diameter of 90mm of outer barrel contraction section lower ending opening,
35 ° of the angle of throat (acute angle of direct tube section and taper type contraction section) of outer barrel lower part taper type contraction section.Baffle spindle
The a diameter of 150mm of axial cross section maximum.Using kerosene as liquid, oil inlet quantity is 60~120L/hr；Gas phase selects nitrogen,
Air inflow is 2~4Nm3/hr.It is the aluminum oxide micro-sphere catalyst of 0.7~0.8mm that solid phase, which selects grain size, and catalyst inventory is (with quiet
Counted when only) it is the 55~80% of reactor dischargeable capacity (disregarding end socket space).Test result is shown in Table 1.
1 cold model unit test result of table
From cold model experiment as can be seen that the utility model fluidized bed reactor has good solid separating effect, it is applicable in
Operating range it is wider.
Claims (9)
1. a kind of boiling bed hydrogenation consersion unit, it is characterised in that：Including boiling bed hydrogenation reactor, catalyst be added system and
Add agent pipeline (1), wherein it includes that catalyst storage tank (2) and connection catalyst storage tank (2) add with ebullated bed that system, which is added, in catalyst
The catalyst delivery line (3) of hydrogen reactor inner space, is arranged at least two valves (4) on catalyst delivery line (3), and two
Catalyst delivery line (3) between a valve (4) with plus agent pipeline (1) between be connected to using anti-hydrogen sulfide leakage pipeline (5),
At least one valve (4) is set on anti-hydrogen sulfide leakage pipeline (5).
2. boiling bed hydrogenation consersion unit according to claim 1, it is characterised in that：The boiling bed hydrogenation reactor
Three phase separator including shell (6) and positioned at shell (6) internal upper part, three phase separator includes two different concentric circles of internal diameter
The upper and lower ends of cylinder, i.e. inner cylinder (7) and outer barrel (8), inner cylinder (7) and outer barrel (8) are all open, and the upper end opening of outer barrel (8) is low
Upper end opening in inner cylinder (7), the lower ending opening of outer barrel (8) are less than the lower ending opening of inner cylinder (7), and outer barrel (8) top is straight tube
Section, outer barrel (8) lower part be a taper type contraction section, the lower ending opening of lower ending opening, that is, outer barrel (8) of contraction section, inner cylinder (7)
Gap is provided between lower ending opening and outer barrel (8) contraction section, shell (6) is the cylinder type shell (6) perpendicular to horizontal plane, shell
Body (6), inner cylinder (7) and outer barrel (8) are concentric setting, and outer barrel (8) is fixed on by support construction on shell (6) inner wall, interior
Cylinder (7) is fixed on by support construction on outer barrel (8) inner wall, and the top in inner cylinder (7) is provided with liquid discharge tube line (9), shell
Body (6) top is provided with liquid outlet (10), and liquid discharge tube line (9) is connected with liquid outlet (10), and the lower end of outer barrel (8) is opened
The lower section setting baffle (11) of mouth, shell (6) interior lower part are provided with distribution plate (12), and being provided with gas at the top of shell (6) goes out
Mouth (13), shell (6) bottom is provided with material inlet (14) and catalyst outlet (15).
3. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：The direct tube section of the outer barrel (8)
Internal diameter be shell (6) internal diameter 50~90%.
4. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：The inner cylinder (7) and outer barrel (5)
Between annular space distance be outer barrel (8) corresponding position radius 30~70%.
5. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：Inner cylinder (7) upper end with it is outer
The difference in height of cylinder (8) upper end is the 10~50% of outer barrel (8) radius.
6. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：It opens the lower end of the inner cylinder (7)
Gap between mouth and outer barrel (8) contraction section is the 5~40% of outer barrel (8) direct tube section radius.
7. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：Under described outer barrel (8) contraction section
The 10~50% of a diameter of outer barrel of end opening (8) direct tube section diameter.
8. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：Described outer barrel (8) contraction section
Angle of throat angle is 20 °~80 °.
9. boiling bed hydrogenation consersion unit according to claim 2, it is characterised in that：The baffle (11) is up and down
Spindle small in ends, broad in the middle, the 1~3 of a diameter of outer barrel of spindle axial cross section maximum (8) lower ending opening diameter
Times.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201820188358.5U CN207933355U (en) | 2018-02-02 | 2018-02-02 | Boiling bed hydrogenation consersion unit |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820188358.5U CN207933355U (en) | 2018-02-02 | 2018-02-02 | Boiling bed hydrogenation consersion unit |
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| CN207933355U true CN207933355U (en) | 2018-10-02 |
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ID=63651225
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2018
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| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20181029 Address after: 200120 104, room 1, 2555 Xiu Pu Road, Pudong New Area, Shanghai. Patentee after: Shanghai Jun Ming Chemical Engineering Design Co. Ltd. Address before: 201400 1278, room 6, 1150 LAN Feng Road, Fengxian District, Shanghai. Patentee before: SHANGHAI YINGBAO ENERGY CHEMICAL TECHNOLOGY CO., LTD. |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190402 Address after: 200120 104, room 1, 2555 Xiu Pu Road, Pudong New Area, Shanghai. Co-patentee after: LANZHOU LS HEAVY EQUIPMENT CORPORATION LTD. Patentee after: Shanghai Jun Ming Chemical Engineering Design Co. Ltd. Address before: 200120 104, room 1, 2555 Xiu Pu Road, Pudong New Area, Shanghai. Patentee before: Shanghai Jun Ming Chemical Engineering Design Co. Ltd. |
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| TR01 | Transfer of patent right |