CN204583141U - The controlled water shifting heat reactor of a kind of double-seal head - Google Patents
The controlled water shifting heat reactor of a kind of double-seal head Download PDFInfo
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- CN204583141U CN204583141U CN201520100862.1U CN201520100862U CN204583141U CN 204583141 U CN204583141 U CN 204583141U CN 201520100862 U CN201520100862 U CN 201520100862U CN 204583141 U CN204583141 U CN 204583141U
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- head
- end socket
- heat exchanger
- exchanger tube
- gas
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Abstract
The utility model discloses the controlled water shifting heat reactor of a kind of double-seal head, the top of main cylinder connects lower flange, and the bottom of main cylinder connects lower outside head, and upper flange is connected with lower flange; One end of described Catalyst packing pipe is connected between interior end socket and gas distributing cylinder, the other end is successively through dividing plate and upper outside head, described aqueduct one end is communicated between dividing plate and upper outside head, the other end is set in heat exchanger tube, the body of described heat exchanger tube is positioned at gas distributing cylinder, the outlet of heat exchanger tube dividing plate and between end socket, the cylindrical shell of described gas collecting jar with ground-on cover plate is positioned at gas distributing cylinder, and the outlet of gas collecting jar with ground-on cover plate connects gas outlet.Heat exchanger tube is embedded in beds inside beds internal-response heat to be removed in time, efficiently solves catalyst short, the easy overtemperatures in service life such as existing conversion, synthesis and hydrogenation, side reaction thing is many, bed temperature is wayward, the driving time is long, be difficult to defects such as maximizing, operation energy consumption is high, construction investment is large.
Description
Technical field
The utility model relates to a kind of fixed bde catalyst, the conversion under gas phase state, synthesis, hydrogenation reactor, in particular the controlled water shifting heat reactor of a kind of double-seal head.
Background technology
After CO transformationreation, device is as a kind of extensive use reactor of chemical industry, therebetween, people have carried out improvement repeatedly to shift-converter, by original holoaxial to change into overall diameter to, very good effect is obtained in catalyst bed layer resistance, but beds is still adiabatic reaction, and beds is divided into some beds, takes indirect heat exchange or use Technology Quenched with Water between every bed.It is low that this indirect heat exchange reclaims transformation system heat quality, reclaims sensible heat and latent heat efficiency is low, the easy overtemperature of catalyst, convert and be also mixed with the defects such as side reaction such as methanation simultaneously.
The carbonylation synthesis reactor of coal-ethylene glycol, loading catalyst in the pipe of current employing ф 25X2, pipe external application water shifting heat, a shell-and-tube reactor is made up of to ф 21 cylinder shape catalyst bed thousands of holoaxial, distribution of gas is uneven, side reaction thing is many, catalyst bed layer resistance is large, thermal stress is large, equipment leakage, the carbonylation synthesis reactor of glycol unit of a set of 200,000 tons/year need the parallel running of 6 shell reactors, the defects such as construction investment is large.
The esterification hydrogenation reactor of coal-ethylene glycol, loading catalyst in the pipe of current employing ф 38X2, pipe external application water shifting heat, the defects such as a shell-and-tube reactor is made up of to ф 34 cylinder shape catalyst bed thousands of holoaxial, and distribution of gas is uneven, side reaction thing is many, catalyst bed layer resistance is large, thermal stress large, equipment leakage, construction investment are large.
At present, the reaction of coal preparing natural gas adopts: the heat-removing way of n adiabatic bed+n useless overheated boiler, and need to increase reactants water steam to suppress first, second adiabatic bed reaction, configuration cycles gas simultaneously, otherwise there is first, second adiabatic bed temperature runaway phenomenon, the defects such as operation energy consumption is high, plant investment is large, SR is large.
At present, the Fischer-Tropsch synthesis of coal liquifaction, coal paraffin is not also at the maximization device of operation, the small-sized F-T synthesis device reaction device that part is being run also is shell and tube reactor, Fe (or Co) series catalysts is seated in ф 76X4 pipe, still has that distribution of gas is uneven, overtemperature, carbon distribution, Long carbon chain alkane yield are low, resistance is large, equipment leakage, is difficult to the defects such as maximization.
Utility model content
The purpose of this utility model is to overcome the deficiencies in the prior art, provide the controlled water shifting heat reactor of a kind of double-seal head, utilize water in heat exchanger tube to be converted into steam generation decalescence principle and remove heat of reaction in beds in time, and the saturated vapor under by-product different pressures.
The utility model is achieved through the following technical solutions, the utility model comprises the Catalyst packing pipe, water inlet pipe, upper outside head, dividing plate, outlet pipe, at least one aqueduct, at least one heat exchanger tube, upper interior end socket, upper flange, gas distributing cylinder, gas collecting jar with ground-on cover plate, lower interior end socket and the catalyst self-unloading pipe that are connected as a single entity, the lower flange be connected as a single entity, main cylinder, lower outside head, catalyst self-unloading mouth, air inlet and gas outlet, described water inlet pipe is opened in the top of outside head, dividing plate is arranged between outside head and upper interior end socket, described outlet pipe is arranged between dividing plate and upper interior end socket, the bottom of described upper outside head, the upper bottom of interior end socket and the top of gas distributing cylinder are connected on upper flange, the bottom of described gas distributing cylinder is connected on lower interior end socket, described gas distributing cylinder is set in main cylinder, the top of described main cylinder connects lower flange, the bottom of main cylinder connects lower outside head, and upper flange is connected with lower flange, one end of described Catalyst packing pipe is connected between interior end socket and gas distributing cylinder, the other end is successively through dividing plate and upper outside head, described aqueduct one end is communicated between dividing plate and upper outside head, the other end is set in heat exchanger tube, the body of described heat exchanger tube is positioned at gas distributing cylinder, the outlet of heat exchanger tube dividing plate and between end socket, the cylindrical shell of described gas collecting jar with ground-on cover plate is positioned at gas distributing cylinder, the outlet of gas collecting jar with ground-on cover plate connects gas outlet, described catalyst self-unloading mouth, air inlet and gas outlet are arranged in lower outside head respectively, described catalyst self-unloading pipe one end is connected on lower interior end socket, the other end is connected on catalyst self-unloading mouth.
As one of preferred embodiment of the present utility model, arrange short circuit extend neck between described upper outside head and upper flange, described outlet pipe is arranged on short circuit extend neck, and one end of short circuit extend neck connects upper outside head, the other end is fixed on upper flange, and dividing plate is between short circuit extend neck and upper outside head.
As one of preferred embodiment of the present utility model, described heat exchanger tube is the structure that one end open is closed in one end, body and the blind end of heat exchanger tube are positioned at gas distributing cylinder, and the openend of heat exchanger tube is arranged between dividing plate and upper interior end socket, and described aqueduct is set in heat exchanger tube.
As one of preferred embodiment of the present utility model, described interior end socket is flexible tubesheet or standard sealing head, and described standard sealing head is selected from the one in dome head, ellipse head, conical head, butterfly end socket, ball crown type end socket.As one of preferred embodiment of the present utility model, described interior end socket and short circuit extend neck are welded on upper flange respectively.
As one of preferred embodiment of the present utility model, described upper flange is special-shaped flange, and described special-shaped flange is standard flange or nonstandard of flanges.
As one of preferred embodiment of the present utility model, described upper flange is connected by securing member with lower flange, is provided with gasket seal between upper flange and lower flange.
As one of preferred embodiment of the present utility model, described gasket seal is Ω gasket seal.
As one of preferred embodiment of the present utility model, described gas distributing cylinder is provided with multiple air admission hole.
As one of preferred embodiment of the present utility model, the cylindrical shell of described gas collecting jar with ground-on cover plate is provided with multiple gas collection hole.
The utility model is for CO transformationreation reactor existing problems and deficiency, and present high water/gas, high CO Water gas shift/WGS demand, develop the controlled water shifting heat shift-converter of double-seal head, employing heat exchanger tube is embedded in transformation catalyst bed, utilizes water in heat exchanger tube to be converted into steam generation decalescence principle by CO+H
2o → H
2+ CO
2+ Q
putheat is released in transformationreation, and shifts out beds in time, guarantees reaction bed temperature≤380 DEG C, and the saturated vapor of by-product 0.8 ~ 9.0MPa, is beneficial to catalyst self-unloading and is convenient to the maintenance of heat exchanger tube part.Efficiently solve existing shift-converter reclaim heat quality low, reclaim low, the easy overtemperature of catalyst of heat energy efficiency, methanation side reaction, the difficult self-unloading of catalyst and the large defect of construction investment.
The utility model is for filling Pd/AI
2o
3the carbonylation shell and tube synthesis reactor existing problems of series catalysts, ethylene glycol and deficiency, develop double-seal head controlled water shifting heat carbonyl compound reactor, employing heat exchanger tube is embedded in transformation catalyst bed by employing, utilizes water in heat exchanger tube to be converted into steam generation decalescence principle by CO+CH
3oNO → (COOCH
3)
2+ NO+Q
putreaction is released heat and is shifted out beds in time, guarantees reaction bed temperature≤140 DEG C, and the saturated vapor of by-product 0.2 ~ 0.3MPa, beds adopts full radial structure.Efficiently solve existing carbonylation synthesis reactor catalyst easy overtemperature, side reaction be large, bed resistance is large, be difficult to maximize, catalyst difficulty self-unloading and the large defect of construction investment.
The utility model has problems and deficiency for the esterification hydrogenation shell and tube synthesis reactor of filling Cu series catalysts, ethylene glycol, develop the controlled water shifting heat hydrogenation reactor of double-seal head, employing heat exchanger tube is embedded in transformation catalyst bed by employing, utilizes water in heat exchanger tube to be converted into steam generation decalescence principle by CH
3oNO adds H
2reaction (4H
2+ (COOCH
3)
2→ (OHCH
2c H
2oH)
2+ 2CH
3oH+Q
put) release heat and shift out beds in time, guarantee reaction bed temperature≤250 DEG C, and the saturated vapor of by-product 1.8 ~ 3.2MPa, beds adopts full radial structure.Efficiently solve the easy overtemperature of existing esterification hydrogenation reactor catalyst, side reaction is large, bed resistance is large, be difficult to maximization, the difficult self-unloading of catalyst and the large defect of construction investment.
The utility model has developed the Ni series catalysts 320 ~ 420 DEG C of serviceability temperatures for inner catalyst unit of state, develop the controlled water shifting heat methane synthesis reactor of double-seal head, employing heat exchanger tube is embedded in transformation catalyst bed by employing, utilizes water in heat exchanger tube to be converted into steam generation decalescence principle by CO and H
2methanation reaction (CO+H
2→ CH
4+ H
2o+Q
put) release heat and shift out beds in time, guarantee reaction bed temperature≤420 DEG C, and the saturated vapor of by-product 3.8 ~ 12.0MPa, beds adopts full radial structure.The defect such as efficiently solve the easy overtemperature of existing methane synthesis reactor catalyst, bed resistance is large, operation energy consumption is high, plant investment is large, SR is large.
The utility model has problems and deficiency for the Fischer-Tropsch shell and tube synthesis reactor of filling Fe (or Co) series catalysts, develop double-seal head controlled water shifting heat Fischer-Tropsch synthesis device, employing heat exchanger tube is embedded in transformation catalyst bed by employing, utilizes water in heat exchanger tube to be converted into steam generation decalescence principle by CO and H
2fischer-Tropsch synthesis (nCO+ (2n+1) H
2→ C
nh
2n+2+ nH
2o+Q
put) release heat and shift out beds in time, guarantee Co reaction bed temperature≤240 DEG C, and the saturated vapor of by-product 1.8 ~ 2.8MPa; Fe reaction bed temperature≤260 DEG C, and the saturated vapor of by-product 1.6 ~ 3.8MPa, beds adopts full radial structure.Efficiently solve the defect that existing Fischer-Tropsch synthesis device exists.
The utility model has the following advantages compared to existing technology: the utility model inlet distribution, catchment, assembly that the catalytic reaction Trinity can be lifted by crane separately is separated with outer cylinder body, easy access, catalyst self-unloading, Catalyst packing;
Heat exchanger tube is embedded in beds inside beds internal-response heat to be removed in time, avoid original conversion, synthesis and hydrogenation catalyst to be sintered phenomenon to occur, efficiently solve catalyst short, the easy overtemperatures in service life such as existing conversion, synthesis and hydrogenation, side reaction thing is many, bed temperature is wayward, the driving time is long, be difficult to defects such as maximizing, operation energy consumption is high, construction investment is large;
The temperature of beds is regulated by byproduct steam pressure, guarantees that adjustment aspect is flexible, easy to control; When also guaranteeing to drive simultaneously, take to add steam to water circulation system, rapidly the temperature rise of controlled for a kind of double-seal head water shifting heat reactor is got up, with restart up;
Natural Circulation is taked in water route, during unexpected parking, the reactant of inside reactor nubbin of the present utility model continues reaction, water route also still keeps circulation, and beds internal heat is shifted out, guarantee also can not surpass at the bed temperature of the controlled water shifting heat reactor of a kind of double-seal head of unexpected dead ship condition, available protecting catalyst service life;
Gas distributing cylinder of the present utility model and gas collecting jar with ground-on cover plate, adopt bidirectional compensating between inside and outside reactor, makes radial gas distribution error≤5.0%, guarantees that distribution of gas is even; Reactor bed overall resistance≤0.01MPa;
Adopt overall diameter to beds, be easy to larger-scale unit, not only solve a transport difficult problem, reduce construction investment simultaneously.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model.
Detailed description of the invention
Below embodiment of the present utility model is elaborated; the present embodiment is implemented under premised on technical solutions of the utility model; give detailed embodiment and concrete operating process, but protection domain of the present utility model is not limited to following embodiment.
As shown in Figure 1, the present embodiment comprises the Catalyst packing pipe 2, water inlet pipe 3, upper outside head 4, dividing plate 6, outlet pipe 7, multiple aqueduct 18, multiple heat exchanger tube 19, upper interior end socket 10, upper flange 11, gas distributing cylinder 16, gas collecting jar with ground-on cover plate 20, lower interior end socket 23 and the catalyst self-unloading pipe 27 that are connected as a single entity, the lower flange 13 be connected as a single entity, main cylinder 15, lower outside head 24, catalyst self-unloading mouth 29, air inlet 25 and gas outlet 28;
Water inlet pipe 3 is opened in the top of outside head 4, dividing plate 6 is arranged between outside head 4 and upper interior end socket 10, outlet pipe 7 is arranged between dividing plate 6 and upper interior end socket 10, between upper outside head 4 and upper flange 11, short circuit extend neck 9 is set, outlet pipe 7 is arranged on short circuit extend neck 9, and one end of short circuit extend neck 9 connects upper outside head 4, and the other end is fixed on upper flange 11, dividing plate 6 is between short circuit extend neck 9 and upper outside head 4, and short circuit extend neck 9 is convenient to device distribution, in upper, end socket 10 and short circuit extend neck 9 are welded on upper flange 11 respectively, the top of gas distributing cylinder 16 is connected on upper flange 11, the bottom of gas distributing cylinder 16 is connected on lower interior end socket 23, gas distributing cylinder 16 is set in main cylinder 15, the top of main cylinder 15 connects lower flange 13, the bottom of main cylinder 15 connects lower outside head 24, and upper flange 11 is connected with lower flange 13, one end of Catalyst packing pipe 2 is connected between interior end socket 10 and gas distributing cylinder 16, the other end is successively through dividing plate 6 and upper outside head 4, Catalyst packing pipe 2 top be positioned at outside outside head 4 is provided with Catalyst packing mouth 1, aqueduct 18 one end is communicated between dividing plate 6 and upper outside head 4, the other end is set in heat exchanger tube 19, the body of heat exchanger tube 19 is positioned at gas distributing cylinder 16, the outlet of heat exchanger tube 19 dividing plate 6 and between end socket 10, the cylindrical shell of gas collecting jar with ground-on cover plate 20 is positioned at gas distributing cylinder 16, the outlet of gas collecting jar with ground-on cover plate 20 connects gas outlet 28 by escape pipe 26, catalyst self-unloading mouth 29, air inlet 25 and gas outlet 28 are arranged in lower outside head 24 respectively, catalyst self-unloading pipe 27 one end is connected on lower interior end socket 23, the other end is connected on catalyst self-unloading mouth 29.
In the present embodiment, Catalyst packing pipe 2, upper outside head 4, dividing plate 6 and aqueduct 18 constitute inlet distribution room 5, dividing plate 6, upper interior end socket 10, upper flange 11, outlet pipe 7 and heat exchanger tube 19 constitute collecting chamber 8, in upper, end socket 10, upper flange 11, gas distributing cylinder 16, heat exchanger, lower interior end socket 23 constitute catalyst frame 22, upper flange 11, lower flange 13, outer cylinder body, lower outside head 24, lower interior end socket 23, air inlet 25 and gas outlet 28 constitute distribution of gas room 17, and the space in gas collecting jar with ground-on cover plate 20 forms collection chamber 21.
Heat exchanger tube 19 is for closing the structure of one end open in one end, and the body of heat exchanger tube 19 and blind end are positioned at gas distributing cylinder 16, and the openend of heat exchanger tube 19 is arranged between dividing plate 6 and upper interior end socket 10, and aqueduct 18 is set in heat exchanger tube 19.
Upper flange 11 is connected by securing member 14 with lower flange 13, is provided with Ω gasket seal 12 between upper flange 11 and lower flange 13.Gas distributing cylinder 16 is provided with multiple air admission hole.The cylindrical shell of gas collecting jar with ground-on cover plate 20 is provided with multiple gas collection hole.
The upper interior end socket 10 of the present embodiment is made for flexible tubesheet, and the upper interior end socket 10 in other embodiments also can be standard sealing head, and standard sealing head is selected from the one in dome head, ellipse head, conical head, butterfly end socket, ball crown type end socket.
The upper flange 11 of the present embodiment is the special-shaped flange of nonstandard of flanges.
Gas enters distribution of gas room 17 by air inlet 25, enters catalyst frame 22 react in distribution of gas room 17 by gas distributing cylinder 16, and in the hollow cylinder that reaction releasing heat is formed by aqueduct 18 and heat exchanger tube 19, water absorbs.Go out catalyst frame 22 to react rear gas and enter collection chamber 21, escape pipe 26 by gas collecting jar with ground-on cover plate 20, then by escape pipe 26 outflow reactor; Unsaturated water enters inlet distribution room 5 by water inlet pipe 3, then aqueduct 18 is evenly distributed to, flow from top to bottom in aqueduct 18 inside, bottom aqueduct 18, flow out upset 180 ° flow from bottom to top in the hollow cylinder that aqueduct 18 and heat exchanger tube 19 are formed, and absorption heat-exchange pipe 19 external catalyst bed heat, form supersaturation water and enter collecting chamber 8, then enter extraneous drum by outlet pipe 7 outflow reactor, and flash off saturated vapor in drum.Fig. 1 hollow core arrow is water (flow) direction, and filled arrows is airflow direction.
The foregoing is only preferred embodiment of the present utility model; not in order to limit the utility model; all do within spirit of the present utility model and principle any amendment, equivalent to replace and improvement etc., all should be included within protection domain of the present utility model.
Claims (10)
1. the controlled water shifting heat reactor of double-seal head, it is characterized in that, comprise the Catalyst packing pipe (2) be connected as a single entity, water inlet pipe (3), upper outside head (4), dividing plate (6), outlet pipe (7), at least one aqueduct (18), at least one heat exchanger tube (19), end socket (10) in upper, upper flange, gas distributing cylinder (16), gas collecting jar with ground-on cover plate (20), end socket (23) and catalyst self-unloading pipe (27) in lower, the lower flange (13) be connected as a single entity, main cylinder (15), lower outside head (24), catalyst self-unloading mouth (29), air inlet (25) and gas outlet (28), described water inlet pipe (3) is opened in the top of outside head (4), dividing plate (6) is arranged between outside head (4) and upper interior end socket (10), described outlet pipe (7) is arranged between dividing plate (6) and upper interior end socket (10), the bottom of described upper outside head (4), in upper, the bottom of end socket (10) and the top of gas distributing cylinder (16) are connected on upper flange (11), the bottom of described gas distributing cylinder (16) is connected on lower interior end socket (23), described gas distributing cylinder (16) is set in main cylinder (15), the top of described main cylinder (15) connects lower flange (13), the bottom of main cylinder (15) connects lower outside head (24), upper flange (11) is connected with lower flange (13), one end of described Catalyst packing pipe (2) is connected between interior end socket (10) and gas distributing cylinder (16), the other end is successively through dividing plate (6) and upper outside head (4), described aqueduct (18) one end is communicated between dividing plate (6) and upper outside head (4), the other end is set in heat exchanger tube (19), the body of described heat exchanger tube (19) is positioned at gas distributing cylinder (16), the outlet of heat exchanger tube (19) is positioned between dividing plate (6) and upper end socket (10), the cylindrical shell of described gas collecting jar with ground-on cover plate (20) is positioned at gas distributing cylinder (16), the outlet of gas collecting jar with ground-on cover plate (20) connects gas outlet (28), described catalyst self-unloading mouth (29), air inlet (25) and gas outlet (28) are arranged in lower outside head (24) respectively, described catalyst self-unloading pipe (27) one end is connected on lower interior end socket (23), the other end is connected on catalyst self-unloading mouth (29).
2. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, it is characterized in that, between described upper outside head (4) and upper flange (11), short circuit extend neck (9) is set, described outlet pipe (7) is arranged on short circuit extend neck (9), one end of short circuit extend neck (9) connects upper outside head (4), the other end is fixed on upper flange (11), and dividing plate (6) is positioned between short circuit extend neck (9) and upper outside head (4).
3. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, it is characterized in that, described heat exchanger tube (19) is for closing the structure of one end open in one end, the body of heat exchanger tube (19) and blind end are positioned at gas distributing cylinder (16), the openend of heat exchanger tube (19) is arranged between dividing plate (6) and upper interior end socket (10), and described aqueduct (18) is set in heat exchanger tube (19).
4. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, it is characterized in that, described interior end socket (10) is flexible tubesheet or standard sealing head, and described standard sealing head is selected from the one in dome head, ellipse head, conical head, butterfly end socket, ball crown type end socket.
5. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described interior end socket (10) and short circuit extend neck (9) are welded on upper flange (11) respectively.
6. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described upper flange (11) is special-shaped flange, and described special-shaped flange is standard flange or nonstandard of flanges.
7. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, it is characterized in that, described upper flange (11) is connected by securing member (14) with lower flange (13), is provided with gasket seal between upper flange (11) and lower flange (13).
8. the controlled water shifting heat reactor of a kind of double-seal head according to claim 7, is characterized in that, described gasket seal is Ω gasket seal (12).
9. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, described gas distributing cylinder (16) is provided with multiple air admission hole.
10. the controlled water shifting heat reactor of a kind of double-seal head according to claim 1, is characterized in that, the cylindrical shell of described gas collecting jar with ground-on cover plate (20) is provided with multiple gas collection hole.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520100862.1U CN204583141U (en) | 2015-02-11 | 2015-02-11 | The controlled water shifting heat reactor of a kind of double-seal head |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520100862.1U CN204583141U (en) | 2015-02-11 | 2015-02-11 | The controlled water shifting heat reactor of a kind of double-seal head |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204583141U true CN204583141U (en) | 2015-08-26 |
Family
ID=53919342
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520100862.1U Withdrawn - After Issue CN204583141U (en) | 2015-02-11 | 2015-02-11 | The controlled water shifting heat reactor of a kind of double-seal head |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204583141U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104645897A (en) * | 2015-02-11 | 2015-05-27 | 南京敦先化工科技有限公司 | Dual-seal-head controllable water heat removing reactor |
| CN110538615A (en) * | 2019-10-10 | 2019-12-06 | 江苏永大化工机械有限公司 | Ethylene glycol synthetic tower |
-
2015
- 2015-02-11 CN CN201520100862.1U patent/CN204583141U/en not_active Withdrawn - After Issue
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104645897A (en) * | 2015-02-11 | 2015-05-27 | 南京敦先化工科技有限公司 | Dual-seal-head controllable water heat removing reactor |
| CN110538615A (en) * | 2019-10-10 | 2019-12-06 | 江苏永大化工机械有限公司 | Ethylene glycol synthetic tower |
| CN110538615B (en) * | 2019-10-10 | 2021-08-20 | 江苏永大化工机械有限公司 | Ethylene glycol synthetic tower |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20150826 Effective date of abandoning: 20160504 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |