CN208389980U - Beam tube water bed type ethylene glycol hydrogenator - Google Patents
Beam tube water bed type ethylene glycol hydrogenator Download PDFInfo
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- CN208389980U CN208389980U CN201820636352.XU CN201820636352U CN208389980U CN 208389980 U CN208389980 U CN 208389980U CN 201820636352 U CN201820636352 U CN 201820636352U CN 208389980 U CN208389980 U CN 208389980U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The utility model discloses beam tube water bed type ethylene glycol hydrogenators, it includes shell and the intracorporal support component of shell, the inner cavity of shell is divided into upper cavity part and lower cavity part by support component, upper cavity part is provided with a radial conversion zone, lower cavity part is provided with Axial response section, radial conversion zone has the synthesis gas air inlet pipe for being provided with qi-emitting hole, heat exchanger tube is disposed with around synthesis gas air inlet pipe, flowing hole is provided in support component, radial conversion zone is connected to axial conversion zone through the flowing hole, and syngas outlet pipe is connected to axial conversion zone；Catalyst is filled in radial conversion zone and Axial response section.When using reactor in the application, it is only necessary to use a reactor, that is, can guarantee the transformation efficiency of dimethyl oxalate, thus the expenditure of construction of ethylene glycol process units can be reduced, and the quantity of technological parameter is thus reduced, fault rate is reduced, the stability of production is improved.
Description
Technical field
The utility model is specifically related to a kind of beam tube water bed type ethylene glycol hydrogenator.
Background technique
Hydrogenation of Dimethyl Oxalate generates the important channel that ethylene glycol is ethylene glycol preparation, dimethyl oxalate conversion ratio
Height directly influences the construction cost and operational efficiency of device, not bad maximum while guaranteeing dimethyl oxalate conversion ratio
Reduce to limit the generation of side reaction.In current hydrogenation reaction device, for the conversion ratio for improving dimethyl oxalate, generally all adopt
It is produced with the more concatenated modes of reactor, but the concatenated mode of this more reactors not only increases the throwing of equipment
Rate are used, and need to add hydrogen in each reactor in process of production, this lengthens the process of reaction, control point
Increase, is unfavorable for the stability contorting of production.
Utility model content
For the production procedure for simplifying ethylene glycol, the investment cost of ethylene glycol process units is reduced, present applicant proposes one kind
Reactor, the reactor, the reactor can guarantee the conversion ratio of dimethyl oxalate, specific skill on the basis of single device
Art scheme is as follows:
Beam tube water bed type ethylene glycol hydrogenator comprising shell and be mounted on the intracorporal support component of shell, support group
The inner cavity of shell is divided into upper cavity part and lower cavity part by part, and upper cavity part is provided with a radial conversion zone, is provided in lower cavity part
1-4 Axial response section；Synthesis gas inlet pipe and steam water interface outlet are installed in the upper end of shell, in the lower end of shell
Syngas outlet pipe is installed, is provided with hot water inlet pipe on the side wall of shell；
The radial direction conversion zone includes the synthesis gas air inlet pipe for being mounted on the center of upper cavity part, the upper end of synthesis gas air inlet pipe to
Upper extension is connected to the synthesis gas inlet pipe, is provided with qi-emitting hole in synthesis gas air inlet pipe；
Heat exchanger tube is disposed with around synthesis gas air inlet pipe, one end of heat exchanger tube is connected to steam water interface outlet, changes
The other end of heat pipe is connected to hot water inlet pipe；
Corresponding to each Axial response section, the axial direction part discharging of the connection Axial response section is provided on shell
Pipe；
The radial section discharge duct of a connection radial direction conversion zone is provided on shell；
Flowing hole is provided in support component, radial conversion zone is connected to axial conversion zone through the flowing hole, and synthesis gas goes out
Mouth pipe is connected to axial conversion zone；
The first catalyst is filled in radial conversion zone, the filling height of the first catalyst is radial conversion zone height
85-92%；
The second catalyst is filled in each Axial response section, the filling height of the second catalyst is that all axial directions are anti-
Answer the 91-95% of section total height.
In this application, the inner cavity of shell is divided into upper cavity part and lower cavity part, a radial direction is provided in upper cavity part
Conversion zone is provided with Axial response section in lower cavity part, and when the work of this reactor, unstripped gas is entered from synthesis gas inlet pipe
In synthesis gas air inlet pipe, then into being reacted in axial bed, then through flowing hole enter in Axial response section after
Continuous reaction, the gas for completing reaction are discharged from syngas outlet pipe, enter next procedure.
In this reactor, in order to guarantee going on smoothly for reaction, the catalysis in radial conversion zone and Axial response section
The loadings of agent are provided with different filling ratios,, can be in the case where corresponding hydrogen ester ratio under above-mentioned filling ratio
The transformation efficiency of dimethyl oxalate is set to stablize the dimethyl oxalate 99.9% or more, from the reaction mixture gas that reactor is discharged
Content be lower than 5ppm, the yield of ethylene glycol reaches 98% or more.When therefore, using the reactor in the application, it is only necessary to adopt
With a reactor, that is, it can guarantee the transformation efficiency of dimethyl oxalate, thus can reduce the expenditure of construction of ethylene glycol process units,
Simultaneously because reducing the quantity of reactor, the quantity of technological parameter can be efficiently reduced, and thus reduces fault rate, improves life
The stability of production.
In the reactor, in each conversion zone, catalyst is not completely filled up, and still there are certain spaces, due to rigid
The concentration highest of the reaction gas in each conversion zone is entered, it is most fierce to react, can be to catalysis due to there is the presence in above-mentioned space
The top layer of agent quickly supplements a certain amount of unstripped gas, avoids the overreaction of unstripped gas, reduces the probability that side reaction generates.
It further, is 40-50m than huyashi-chuuka (cold chinese-style noodles) product in radial conversion zone2/m3.It is above-mentioned more long-pending than huyashi-chuuka (cold chinese-style noodles) in radial conversion zone
The ratio of the volume of the heat exchange area of heat exchanger tube and the first catalyst.Within the above range than huyashi-chuuka (cold chinese-style noodles) product, it is ensured that reaction thermal energy
It is enough smoothly to be taken away by the hot water in heat exchanger tube, stablize the reaction temperature in reactor within the set range.
Further, an adapter cavity is provided in lower cavity part, Axial response section is arranged in the downside of adapter cavity；The heat
Water inlet pipe is arranged on shell corresponding to adapter cavity.Specifically, radial section discharge duct setting is corresponding to the adapter cavity
Shell on, which is connected to radial conversion zone through the central portion of support component, and first in radial conversion zone urges
Agent can be discharged through the radial section discharge duct.
One special transition region is set, become pipeline by area, and the transition region is alternatively arranged as equipment making
With the operating space of maintenance, make in the maintenance process of equipment, the second catalyst of axial direction part will not be impacted, be ensure that
The overhaul efficiency of equipment.
Further, to avoid reaction gas from forming dead angle in the bottom of lower cavity part, the overreact of part reaction gas is caused, is drawn
A large amount of side reaction is played, the bottom of lower cavity part is provided with an air collecting chamber, Axial response section is arranged in the upside of air collecting chamber, described
Syngas outlet pipe is arranged on shell corresponding to air collecting chamber.After air collecting chamber is arranged, from the reaction gas of Axial response section discharge
It is no longer reacted, efficiently avoids reaction gas in through synthesis gas outlet discharge process, since part reaction gas flow passes through
Overreaction caused by the path of catalyst extends.
To be smoothly discharged out catalyst, the axis of the axial direction part discharge duct of the Axial response section adjacent with air collecting chamber along shell
To downward through shell.Alternatively, radial section discharge duct along inclined direction extends downwardly；When Axial response section is provided at least two
When, in addition to the Axial response section for being located at bottom, the axial discharge duct of remaining Axial response section is arranged on corresponding shell
And along inclined direction downwards, extend outwardly.
Specifically, when Axial response section is provided at least two, there is a cloth air cavity between two adjacent Axial response sections,
Manhole is provided on the shell corresponding to cloth air cavity.After cloth air cavity is set, unreacted unstripped gas weight in unstripped gas can be made
It is newly distributed, to improve reaction efficiency.It, can be in order to each Axial response section be overhauled and is tieed up respectively after manhole is set
Shield, while being also convenient for processing corresponding region.
In the technique using any of the above-described reactor production ethylene glycol, hydrogen ester ratio is 85-97；Hot water is from hot water inlet
Pipe enters in heat exchanger tube, becomes steam water interface after absorbing reaction heat, is then discharged from steam water interface outlet.Hydrogen ester ratio
For the molar ratio of hydrogen and dimethyl oxalate.
Using above-mentioned reactor, and under above-mentioned hydrogen ester ratio and heat exchange state, it can effectively guarantee dimethyl oxalate
Reaction efficiency.The hot water used during removing to reaction heat is heated as steam water interface in heat exchange,
Since water can absorb a large amount of thermal energy during vaporization, rapidly reaction heat can be removed, simultaneously because using
Steam water interface removes reaction heat, it is possible to reduce the usage amount of water is more advantageous to and produces corresponding steam using steam water interface.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of an embodiment of the present invention.
Fig. 2 is the enlarged drawing of part A in Fig. 1.
Specific embodiment
Herein, the axial direction, the i.e. extending direction of the central axis 105 of shell 10 in Fig. 1.
Referring to Fig. 1, a kind of beam tube water bed type ethylene glycol hydrogenator comprising tubular shell 10, shell 10
Including cylindric cylinder 11, the upper cover 12 of 11 upper end of cylinder and the lower head 13 of lower end are set.It is installed in shell 10
There is support component 3, the inner cavity of shell 10 is divided into upper cavity part 101 and lower cavity part 102 by support component 3, is arranged in upper cavity part 101
There is a radial conversion zone, lower cavity part 102 is provided with 2 Axial response sections.Synthesis gas inlet pipe is installed in the upper end of shell
14 and steam water interface outlet 8, syngas outlet pipe 15 is installed in the lower end of shell, is provided with heat on the side wall of shell
Water inlet pipe 2.
The radial direction conversion zone includes synthesis gas air inlet pipe 5, internals 41, heat exchanger tube 61 and catalyst cover plate assembly 43, synthesis gas
Air inlet pipe 5 is mounted on the center of upper cavity part 101, and the upper end of synthesis gas air inlet pipe 5 upwardly extends the connection synthesis gas inlet pipe
14, venthole is provided in synthesis gas air inlet pipe 5.
Specifically in the present embodiment, the lower end of synthesis gas air inlet pipe 5 is resisted against the upper end of following support plates 59, synthesis gas
The upper end of air inlet pipe 5 is extend into synthesis gas inlet pipe 14, is equipped with a flange on the upper surface of synthesis gas inlet pipe 14
141, which is closely held in synthesis gas air inlet pipe 5 in shell.
It is outer and support in support component 3 that internals 41 are set in synthesis gas air inlet pipe 5, heat exchanger tube 61 be arranged in internals 41 with
In region between synthesis gas air inlet pipe 5.
In the present embodiment, the support component 3 includes support ring 31, crosses inflator 32 and catalyst bottom plate 34；Support ring 31
Annularly, the lateral surface of support ring 31 is fixedly connected on the medial surface of cylinder 11 of shell 10, is crossed inflator 32 and is cylindrical in shape, crosses gas
The lower end of cylinder 32 is connected to the inside edge of support ring 31；Catalyst bottom plate 34 was sealingly mounted at the upper end of inflator 32；Please simultaneously
Referring to Fig.2, offering flowing hole 33 on crossing inflator 32, radial conversion zone is connected to axial conversion zone through the flowing hole 33.
Internals 41 are in the tubular of upper and lower opening, and 41 liner of internals is in shell 10 and is located in upper cavity part 102, internals 41
Lower end is sealedly connected in support component 3, makes to form air collecting chamber between internals 41 and shell 10.It is opened up in connection in internals 41
Outer qi-emitting hole, the qi-emitting hole are not shown in figure.Catalyst cover plate assembly 43 is mounted on the upper end of internals 41.
Heat exchanger tube 61 arranges that in the present embodiment, heat exchanger tube 61, which divides, restrains 6 for three around synthesis gas air inlet pipe 5, corresponds to
In the upper interior end socket 72 that each tube bank 6 is provided with internal tube plate 71 on one, is welded on upper internal tube plate 71, on upper interior end socket 72
Steam water interface outlet 8 is set, and steam water interface outlet 8 is specifically mounted on upper cover 12.Corresponding to each tube bank 6
It is provided with internal tube plate 91, the lower interior end socket 92 being welded on lower internal tube plate 91, hot water inlet is set on lower interior end socket 92
Pipe 2, hot water inlet pipe 2 are mounted on cylinder 11.The upper end of heat exchanger tube in each tube bank 6 is welded on internal tube plate 71, under
End is welded on lower internal tube plate 91.The upper end of heat exchanger tube 61 is successively connected to steam water interface after upper internal tube plate 71, interior end socket 72
Outlet 8, the lower end of heat exchanger tube 61 are successively connected to hot water inlet pipe 2 after lower internal tube plate 91, upper internal tube plate 91.
In the present embodiment, catalyst cover plate assembly 43 includes catalyst cover board 44 and the catalyst lid being connected on the inner wall of cylinder 11
Plate supporting member 45, wherein catalyst cover board is supported in catalyst cover support.72 hermetically passing catalyst cover board 44 of end socket in upper, i.e.,
Outlet pipe component hermetically passing catalyst cover plate assembly 43.
In the setting of lower cavity part 102 there are two Axial response section, for convenience of description, two Axial response sections are referred to as the
One Axial response section 17 and the second Axial response section 18, first axis conversion zone 17 are located at the top of the second Axial response section 18.
First axis conversion zone 17 has an axial catalyst support plate 172 and an axial catalyst cover board 171.Second Axial response section 18 tool
There are an axial catalyst support plate 182 and an axial catalyst cover board 181.The shape between first axis conversion zone 17 and support component 3
At an adapter cavity 65, an air collecting chamber 19 is formed between the second Axial response section 18 and lower head 13.Syngas outlet pipe 15 is pacified
Mounted in the bottom of air collecting chamber 19, that is, it is mounted on the bottom of lower head 13.Axial catalyst support plate 172, axial catalyst cover board
171, axial catalyst support plate 182 and axial catalyst cover board 181 offer duct for gas to pass through.
Corresponding to each Axial response section, the axial direction part discharge duct for being connected to the Axial response section is provided on shell；
For convenience of description, axial direction part discharge duct corresponding to first axis conversion zone 17 is known as first axis section discharge duct 173, by
Axial direction part discharge duct corresponding to two Axial response sections 18 is known as the second axial direction part discharge duct 183.
First axis section discharge duct 173 is inclined on cylinder 11, and the import of first axis section discharge duct 173 is located at axis
To the lower end of conversion zone 17, and along inclined direction downwards, extend outwardly.
The upper of axial catalyst support plate 182 is arranged in second axial direction part discharge duct 183, and extends downwardly through lower head
13, the second axial direction part discharge duct 183 is downward through shell 10.
In the present embodiment, two Axial response sections are provided with, when an Axial response section is only arranged, the Axial response
The axial direction part discharge duct of section is downward through lower head.It is axial except the lowermost is located at when 3 or 4 Axial response sections is arranged
Outside conversion zone, the axial direction part discharge duct of remaining Axial response section can refer to setting for above-mentioned first axis section discharge duct 173
The mode of setting is configured.
Reaction efficiency for raising unstripped gas is convenient to overhaul, and a cloth air cavity 66 is provided between two Axial response sections,
A manhole 16 is provided on the shell corresponding to cloth air cavity 66.
Illustrate the mounting means of the radial section discharge duct of radial conversion zone below.It is equipped in the middle part of catalyst bottom plate 34
One top discharge pipe 35, one end of the top discharge pipe 35 are formed after extending upward through catalyst bottom plate into catalyst inlet, top discharge pipe 35
The other end be connected with discharge nozzle 36.Specifically in the present embodiment, the bottom discharge pipe along inclined direction downwards, to extension
It stretches, and is mounted on cylinder 11 corresponding to adapter cavity 65, radial section discharging is collectively formed in top discharge pipe 35 and bottom discharge pipe 36
Pipe, i.e., radial section discharge duct is arranged on shell 10 corresponding to adapter cavity 65, and the radial section discharge duct is through in support component
Centre portion is connected to radial conversion zone, and the first catalyst in radial conversion zone can be discharged through the radial section discharge duct.
It is welded with support plate 59 in the side at the center towards cylinder 10 of lower internal tube plate 91, each on lower internal tube plate 91
It is welded with a support plate 59, support plate 59 extends along the axis direction of shell, and the lower end of support plate 59 is welded on lower internal tube plate,
There is gap between adjacent support plate 59, which forms the tapping channel for being connected to radial conversion zone and top discharge pipe 35,
The tapping channel is connected to radial conversion zone and top discharge pipe 35.
Hot water inlet pipe 2 is arranged on shell 10 corresponding to adapter cavity 65.Hot water inlet pipe 2 includes being connected to lower interior envelope
Bend pipe 21 on first 92 and the hot-water line 211 in straight tube dress being connected on bend pipe 21, hot-water line 211 is horizontally disposed and is welded on
On cylinder 11, one end of hot-water line 211 is stretched out outside cylinder, and one end outside the stretching cylinder of hot-water line 211 is equipped with blind plate 22,
The steam pipe 23 that goes into operation horizontally extends into the inner cavity of hot-water line 211 after blind plate 22, stretches out one outside cylinder 11 in hot-water line 211
The desalted water inlet tube 212 of the inner cavity of connection hot-water line 211 is installed on the upside of end, is stretched out outside cylinder 11 in hot-water line 211
The inner cavity of connection hot-water line 211 is equipped on the downside of one end leads leaching mouth pipe 24.
The first catalyst is filled in radial conversion zone, the filling height of the first catalyst is radial conversion zone height
90%.The second catalyst is filled in each Axial response section, the filling height of the second catalyst is all Axial responses
The 93% of section total height.
It is understood that according to different requirements, the filling height of the first catalyst be can be in radial direction in other embodiments
It is arbitrarily selected between the 85-92% of conversion zone height, such as can be 85%, 87% or 92%；The filling of second catalyst is high
Degree can be and arbitrarily select between the 91-95% of all Axial response section total heights, such as can be 91%, 92% or 94%.
It is 45m than huyashi-chuuka (cold chinese-style noodles) product in radial conversion zone2/m3.It is above-mentioned to be changed than huyashi-chuuka (cold chinese-style noodles) product for heat exchanger tube in radial conversion zone
The ratio of heat area and the volume of the first catalyst.It is appreciated that according to different needs, in other embodiments, it is above-mentioned than cold
Area can be in 40-50m2/m3Between specifically selected, such as can be 40m2/m3、42m2/m3、47m2/m3、49m2/m3
Or 50m2/m3。
In Fig. 1, label 100 indicates the flow direction of unstripped gas in the reactor, specifically: unstripped gas is through synthesis gas air inlet pipe
Venthole on 5 enters the space between synthesis gas air inlet pipe 5 and internals 41, carries out under the action of the first catalyst anti-
It answers, the gaseous mixture after reaction enters air collecting chamber by the qi-emitting hole in internals 41, then enters adapter cavity through flowing hole 33
65, then successively pass through first axis conversion zone 17 and the second Axial response section 18, continue to react, then into air collecting chamber
In 19, finally it is discharged through synthesis gas outlet 15, enters next procedure.
Using the technique of the beam tube water bed type ethylene glycol hydrogenator production ethylene glycol in the present embodiment, in the production second
In the technique of glycol, hydrogen ester ratio is 94, and in process of production, hot water enters in heat exchanger tube from hot water inlet pipe, absorbing reaction
Become steam water interface after heat, is then discharged from steam water interface outlet.
In other embodiments, according to different settings, hydrogen ester ratio can specifically be selected between 85-97, example
It such as can be 85,87,89,91,95 or 97.
In the present embodiment, it is 4.3ppm from the content of the dimethyl oxalate in the reaction mixture gas that reactor is discharged, turns
Rate reaches 99.95%, and the yield of ethylene glycol reaches 98.5%.
Using above-mentioned reactor, when hydrogen ester ratio is set as 85,87,89,91,95 or 97, from the reaction of reactor discharge
The content of dimethyl oxalate in gaseous mixture is below 5ppm, and the yield of ethylene glycol reaches 98% or more.
In the present embodiment, the nominal diameter of reactor is DN4000, and only actual production can substitute two in the prior art
Nominal diameter is the reactor of DN3800, thereby reduces technology controlling and process point, improves the stability of production, and basic herein
On, reduce the gross investment amount of ethylene glycol production system.
Claims (8)
1. beam tube water bed type ethylene glycol hydrogenator, which is characterized in that including shell and it is mounted on the intracorporal support component of shell,
The inner cavity of shell is divided into upper cavity part and lower cavity part by support component, upper cavity part is provided with a radial conversion zone, in lower cavity part
It is provided with 1-4 Axial response section；Synthesis gas inlet pipe and steam water interface outlet are installed in the upper end of shell, in shell
Lower end syngas outlet pipe is installed, be provided with hot water inlet pipe on the side wall of shell；
The radial direction conversion zone includes the synthesis gas air inlet pipe for being mounted on the center of upper cavity part, and the upper end of synthesis gas air inlet pipe is prolonged upwards
The connection synthesis gas inlet pipe is stretched, is provided with qi-emitting hole in synthesis gas air inlet pipe；
Heat exchanger tube is disposed with around synthesis gas air inlet pipe, one end of heat exchanger tube is connected to steam water interface outlet, heat exchanger tube
The other end be connected to hot water inlet pipe；
Corresponding to each Axial response section, the axial direction part discharge duct for being connected to the Axial response section is provided on shell；
The radial section discharge duct of a connection radial direction conversion zone is provided on shell；
Flowing hole is provided in support component, radial conversion zone is connected to axial conversion zone, syngas outlet pipe through the flowing hole
It is connected to axial conversion zone；
The first catalyst is filled in radial conversion zone, the filling height of the first catalyst is the 85- of radial conversion zone height
92%；
The second catalyst is filled in each Axial response section, the filling height of the second catalyst is all Axial response sections
The 91-95% of total height.
2. reactor according to claim 1, which is characterized in that be 40-50m than huyashi-chuuka (cold chinese-style noodles) product in radial conversion zone2/
m3。
3. reactor according to claim 1, which is characterized in that an adapter cavity is provided in lower cavity part, it is axial anti-
Section is answered to be arranged in the downside of adapter cavity；The hot water inlet pipe is arranged on shell corresponding to adapter cavity.
4. reactor according to claim 3, which is characterized in that radial section discharge duct setting is corresponding to the adapter cavity
Shell on, which is connected to radial conversion zone through the central portion of support component, and first in radial conversion zone urges
Agent can be discharged through the radial section discharge duct.
5. reactor according to claim 1, which is characterized in that the bottom of lower cavity part is provided with an air collecting chamber, it is axial
Conversion zone is arranged in the upside of air collecting chamber, and the syngas outlet pipe is arranged on shell corresponding to air collecting chamber.
6. reactor according to claim 5, which is characterized in that the axial direction part of the Axial response section adjacent with air collecting chamber unloads
Expects pipe axially downwardly runs through shell along shell.
7. reactor according to claim 5, which is characterized in that radial section discharge duct along inclined direction extends downwardly；
When Axial response section is provided at least two, in addition to the Axial response section for being located at bottom, remaining Axial response section
Axial discharge duct be arranged on corresponding shell and along inclined direction downwards, extend outwardly.
8. reactor according to claim 1, which is characterized in that adjacent when Axial response section is provided at least two
There is a cloth air cavity between two Axial response sections, be provided with manhole on the shell corresponding to cloth air cavity.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820636352.XU CN208389980U (en) | 2018-04-28 | 2018-04-28 | Beam tube water bed type ethylene glycol hydrogenator |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820636352.XU CN208389980U (en) | 2018-04-28 | 2018-04-28 | Beam tube water bed type ethylene glycol hydrogenator |
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| Publication Number | Publication Date |
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| CN208389980U true CN208389980U (en) | 2019-01-18 |
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ID=65062311
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| CN201820636352.XU Active CN208389980U (en) | 2018-04-28 | 2018-04-28 | Beam tube water bed type ethylene glycol hydrogenator |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108421504A (en) * | 2018-04-28 | 2018-08-21 | 南京聚拓化工科技有限公司 | Beam tube water bed type ethylene glycol hydrogenation reactor and the technique for producing ethylene glycol |
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2018
- 2018-04-28 CN CN201820636352.XU patent/CN208389980U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108421504A (en) * | 2018-04-28 | 2018-08-21 | 南京聚拓化工科技有限公司 | Beam tube water bed type ethylene glycol hydrogenation reactor and the technique for producing ethylene glycol |
| CN108421504B (en) * | 2018-04-28 | 2023-08-01 | 南京聚拓化工科技有限公司 | Beam Guan Shuichuang type ethylene glycol hydrogenation reactor and process for producing ethylene glycol |
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