CN202185300U - Device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in fixed bed by normal butane method - Google Patents
Device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in fixed bed by normal butane method Download PDFInfo
- Publication number
- CN202185300U CN202185300U CN201120300026XU CN201120300026U CN202185300U CN 202185300 U CN202185300 U CN 202185300U CN 201120300026X U CN201120300026X U CN 201120300026XU CN 201120300026 U CN201120300026 U CN 201120300026U CN 202185300 U CN202185300 U CN 202185300U
- Authority
- CN
- China
- Prior art keywords
- fused salt
- temperature
- reactor
- spool
- molten salt
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in a fixed bed by a normal butane method. A slide valve (10) is arranged between a reactor (1) and a fused salt cooler (2), a high temperature fused salt inlet (12) of the slide valve is connected with a fused salt lower circuit of the reactor, an high temperature fused salt outlet (13) is connected with the high temperature fused salt inlet of the fused salt cooler (2) and a low temperature fused salt return opening (20) and a fused salt backflow opening (14) are connected with the fused salt cooler and a fused salt upper circuit of the reactor. The above method is adopted to automatically adjust and control the temperature of the fused salt so as to stabilize the temperature of the fused salt at shell side of the reactor by means of controlling the openness of the slide valve precisely to solve and overcome the temperature fluctuation of reaction. The temperature of the fused salt in the reactor which is originally controlled at +-2-3 DEG C is now controlled precisely in a range of +-0.5 DEG C so that the weight yield of maleic anhydride in the oxidizing reaction is improved by 0.5-1.0%, thereby reducing the content of byproducts in the resultants of the reaction.
Description
Technical field
The present invention relates to maleic anhydride (cis-butenedioic anhydride) production technical field, particularly relate to the fixed bed oxidation reaction temperature of molten salt control and device and the guiding valve regulated.
Background technology
Cis-butenedioic anhydride is a kind of basic important Organic Chemicals commonly used.Be the second largest acid anhydrides raw material that is only second to phthalic anhydride in the world, and its downstream product have development and application prospect quite widely.Cis-butenedioic anhydride is widely used in synthetic resin, lube oil additive, medicine, food additives, 1, a series of important organic chemicals and fine chemicals such as 4-butanediol (BDO), gamma-butyrolacton (GLB), oxolane (THF), succinic acid, fumaric acid.
The core of cis-butenedioic anhydride production technology is high temperature heat release, the gas and solid phase catalyzing oxidation reaction that raw material and air take place in fixed bed reactors.The raw material normal butane fully mixes the back by a certain percentage with air and gets into reactor, in the tubulation that has loaded some catalyst, reacts, and n-butane feed and mist (normal butane+air) ratio is generally 1.6～2.1mol%.The reactor hot(test)-spot temperature is usually at 440～470 ℃.Exothermic heat of reaction is shifted out by fused salt cooler and gas cooler, produces the steam supplying apparatus and uses.Reaction gets into recovery process after generating gas cooled.In oxidation reaction process, normal butane and Air mixing gas get in the reactor tube side, issue angry phase catalytic oxidation at catalyst action, and reactor is a vertical shell/tube-type reactor.In the reactor shell side, adopt a kind of potassium nitrate and natrium nitrosum mixture (fused salt) of fusion, be used as through the pump for liquid salts reciprocation cycle and move hot cooling medium.Exothermic heat of reaction is removed through fused salt, and the part fused salt makes its cooling through the shell side of fused salt cooler through in pipe, producing steam.When normal butane passed through reactor, nearly 82～85% normal butane was participated in reaction, and remainder is converted into CO, CO
2And H
2O.Chemical reaction all is exothermic reaction.Remove CO, CO
2And H
2Outside the O, in reaction, also generate materials such as small amount of acetic acid, acrylic acid.
Mostly fixed bed reactors are tubular structure, and heat transfer area is big, help strong exothermal reaction.For stable reaction is carried out, key is the temperature control of reactor thermophore fused salt.The n butane oxidation reaction belongs to strong exothermal reaction; Yield of maleic anhydride is very responsive to temperature; For large-scale reactor; Under the high load capacity feed conditions, guarantee conversion ratio and high selectivity, key is that temperature of molten salt control is stabilized in the optimum process condition, and realizes that the stable key equipment of temperature of molten salt control is a control valve.Prior art is as shown in Figure 1, between reactor 1 and fused salt cooler 2, is provided with slide valve 4 and control valve 5, the high-temperature molten salt that flows through shell side in the reactor; Some is controlled the fused salt flow of the fused salt cooler of flowing through through the open degree of control valve, and common situation is: control valve adopts pneumatic or electronic dish valve; Control valve is opened precision 1%; Control valve open degree 1 degree (maximum open degree 90 degree), automatic instrument(s) output signal is 4～20mA, cooled low-temperature molten salt mixes the shell side of back Returning reactor with the high-temperature molten salt of circulation; Reach the control exothermic heat of reaction and shift out, realization response device shell side temperature of molten salt stable.Adopt the open degree control method of control valve or manually-operated gate at present; Because characteristics such as fused salt freezing point height, control valve adopt pneumatic or electronic dish valve automatic or manual to regulate control, are non-linear regulation; And dish opening of valves degree is very big to flow effect; The temperature of molten salt undulating value fluctuates reaction temperature at ± 2～3 ℃ thereupon, has influence on oxidation reaction selectivity and yield of maleic anhydride.The reactor temperature of molten salt is usually 400～430 ℃ (initial stage～latter stages).Reactor catalyst bed hot(test)-spot temperature is usually at 430～460 ℃.Oxidizing reaction temperature in the reactor leans on temperature of molten salt control, and temperature of molten salt is controlled by the fused salt flow of the fused salt cooler of flowing through.With this understanding, n-butane conversion is approximately 82～85%.The variation that temperature of molten salt is small can cause the bigger variation of reaction temperature, thereby has influence on conversion ratio and optionally variation, finally has influence on the yield of cis-butenedioic anhydride.Therefore solving the precision control of control valve, make reaction temperature stable, is the key of present cis-butenedioic anhydride production oxidation reaction.
Summary of the invention
In order to solve existing agricultural technology problem; We have done a large amount of work as the proprietary technology unit of cis-butenedioic anhydride production technology to capturing the control valve stable problem, from design, to the production of constructing; Passed through experiment and research many times; Finally developed a kind of normal butane method cis-butenedioic anhydride fixed bed oxidation reaction that is used in, temperature of molten salt control is accurately applied in the actual production with regulating stable guiding valve, the realization temperature of molten salt is regulated control automatically; Solve and overcome reaction temperature and fluctuate, improve oxidation reaction selectivity and yield of maleic anhydride.
Technical scheme of the present invention is following:
A kind of normal butane method maleic anhydride fixed bed oxidizing reaction temperature control set for adjusting of the present invention: like Fig. 2, Fig. 3, shown in Figure 4:
Between reactor 1 and fused salt cooler 2, be provided with guiding valve 10; Circuit is connected under the fused salt of the high-temperature molten salt of guiding valve inlet 12 and reactor 1; High-temperature molten salt outlet 13 is connected with the high-temperature molten salt inlet of fused salt cooler 2, and low-temperature molten salt return port 20 is connected fused salt cooler 2 and reactor 1 with fused salt refluxing opening 14 fused salt cocircuit is connected.Guiding valve of the present invention; Form by valve body 15, expansion joint 16, valve seat 17, spool 18, connecting rod 19 etc.; Be provided with expansion joint 16 in the middle of the valve body, connecting rod 19 connects spool 18 and the auto-controlled electric executing agency 11 above the valve body in valve body, and valve seat 17 is provided with the opening corresponding with spool 18.
Guiding valve of the present invention; Form by valve body 15, expansion joint 16, valve seat 17, spool 18, connecting rod 19 etc.; Be provided with expansion joint 16 in the middle of the valve body, connecting rod 19 connects spool 18 and the auto-controlled electric executing agency 11 above the valve body in valve body, and valve seat 17 is the sleeves that are fixed in the valve body; The position is in the high-temperature molten salt porch, and enters the mouth greater than high-temperature molten salt; Around sleeve, be provided with uniform opening 21, preferred via count is 4～8; In valve seat, be provided with spool; Spool is the sleeve of the valve seat of 2 times of height; The loam cake of spool connects connecting rod 19; The lead to the hole site corresponding with valve seat is provided with spool bore on the sleeve below the middle one deck baffle plate that is provided with of valve cage, baffle plate, and spool bore 18 is the holes that meet the arbitrary shape of linear circulation.Preferably trapezoidal, taper or triangle; The area of spool bore 18 is less than opening 21.Valve seat is that piston is connected with spool.
Method of operating is following:
When (shell side) temperature of molten salt in the reactor departs from the technological parameter controlling value when high or low; Regulate the electric operator 10 that control signal exports guiding valve to through DCS (Distributed Control System); Through connecting rod 19 control spools 18; The stroke aperture of regulating slide valve spool 18 moves up or down spool, changes high-temperature molten salt through the overlapping circulation area of opening on change and the valve seat 17 and exports 13 flows; Reach the fused salt flow of controlling the fused salt cooler of flowing through, realize the purpose of control reactor shell side temperature of molten salt.
In oxidation reaction process; Normal butane and Air mixing gas get in the reactor tube side; Issue angry phase catalytic oxidation at catalyst action; In the reactor shell side, adopt a kind of potassium nitrate and natrium nitrosum mixture of fusion, be used as through the pump for liquid salts reciprocation cycle and move hot cooling medium.Exothermic heat of reaction is removed through fused salt, and the part fused salt makes its cooling through the shell side of fused salt cooler through in pipe, producing steam.
After low-temperature molten salt that high-temperature molten salt behind the gas converting heat of tube side catalytic oxidation and fused salt cooler return mixes; Autoreactor upper, annular passage enters into pump for liquid salts top; Enter into the reactor lower part circular passage through pump for liquid salts (axial-flow type) bottom, and circulate through shell side.Wherein, through the reactor lower part circular passage, a part of fused salt carries out flow-control through guiding valve to be regulated and to enter into fused salt cooler shell side bottom, and produces steam with the boiler water heat exchange of tube side.Cooled low-temperature molten salt is through turning back to reactor upper, annular passage guiding valve top communicating pipe, and enters into pump for liquid salts top behind the high-temperature molten salt hybrid cooling of circulation.
The present invention adopts the guiding valve accuracy control method, reaches temperature of molten salt and regulates control automatically, solves and overcome reaction temperature to fluctuate, and improves oxidation reaction selectivity and yield of maleic anhydride.
Guiding valve implements to regulate automatically controlled condition:
In oxidation reaction process, adopt said method to reach temperature of molten salt and regulate control automatically, through the open degree of accurate control guiding valve, stablizing of realization response device shell side temperature of molten salt solves and overcomes reaction temperature and fluctuate.Make the reactor temperature of molten salt by former control ± 2～3 ℃ be accurate to ± 0.5 ℃ of scope.Improve oxidation reaction selectivity and yield of maleic anhydride, make oxidation reaction cis-butenedioic anhydride weight yield improve 0.5～1.0%, cis-butenedioic anhydride product promptly per ton reduces raw material (normal butane) and consumes 12～14kg.Simultaneously, improve the selectivity of oxidation reaction, reduced the accessory substance in the reaction product.
Description of drawings
Fig. 1: former technological process and adjustment control method;
Fig. 2: technological process of the present invention and adjustment control method;
Fig. 3: guiding valve diagram of the present invention.
Fig. 4: spool sketch map.
Fig. 5: temperature control comparison diagram
The specific embodiment
Adopt like Fig. 2, Fig. 3, normal butane method maleic anhydride fixed bed oxidizing reaction temperature control set for adjusting shown in Figure 4; Between reactor 1 and fused salt cooler 2, be provided with guiding valve 10; Circuit is connected under the fused salt of the high-temperature molten salt of guiding valve inlet 12 and reactor 1; High-temperature molten salt outlet 13 is connected with the high-temperature molten salt inlet of fused salt cooler 2, and low-temperature molten salt return port 20 is connected fused salt cooler 2 and reactor 1 with fused salt refluxing opening 14 fused salt cocircuit is connected.
Guiding valve of the present invention; Form by valve body 15, expansion joint 16, valve seat 17, spool 18, connecting rod 19 etc.; Be provided with expansion joint 16 in the middle of the valve body, connecting rod 19 connects spool 18 and the auto-controlled electric executing agency 11 above the valve body in valve body, and valve seat 17 is provided with the opening corresponding with spool 18.Opening 21 on valve seat 17 can be designed to arbitrary shape with spool 18, meets the hole of linear circulation; Comprise trapezoidal, taper, triangle, rectangle etc.
Method of operating is following:
When (shell side) temperature of molten salt in the reactor departs from the technological parameter controlling value when high or low; Regulate the electric operator 10 that control signal exports guiding valve to through DCS (Distributed Control System); Through connecting rod 19 control spools 18; The stroke aperture of regulating slide valve spool 18 moves up or down spool, changes high-temperature molten salt through the overlapping circulation area of opening on change and the valve seat 17 and exports 13 flows; Reach the fused salt flow of controlling the fused salt cooler of flowing through, realize the purpose of control reactor shell side temperature of molten salt.
According to the embodiment contrast, effect of the present invention is described.
Comparative Examples 1: former technological process explanation
As shown in Figure 1, in oxidation reaction process, normal butane and Air mixing gas get in the reactor tube side, issue angry phase catalytic oxidation at catalyst action, and reactor is a vertical shell/tube-type reactor.In the reactor shell side, adopt a kind of potassium nitrate and natrium nitrosum mixture (fused salt) of fusion, be used as through the pump for liquid salts reciprocation cycle and move hot cooling medium.Reaction heat is removed through fused salt, and the part fused salt makes its cooling through the shell side of fused salt cooler through in pipe, producing steam.
Implement operating mode 1 reaction temperature and regulate control
Basic chemical reaction is following:
Air and normal butane carry out partial oxidation and generate cis-butenedioic anhydride.
The main chemical reactions formula is following:
C4H10+7/2O2→C4H2O3+4H2O
Main side reaction is the normal butane combustion reaction, generates carbon monoxide, carbon dioxide and water:
C4H10+5O2→3CO+CO2+5H2O
When normal butane passed through reactor, nearly 82～85% normal butane was participated in reaction, and remainder is converted into CO, CO2 and H2O.Chemical reaction all is exothermic reaction.Remove CO, outside CO2 and the H2O, in reaction, also generate materials such as small amount of acetic acid, acrylic acid.
The reactor temperature of molten salt is usually at 400～430 ℃.The reactor hot(test)-spot temperature is usually at 430～460 ℃.Oxidizing reaction temperature in the reactor is controlled by the flow through fused salt flow of fused salt cooler of control.With this understanding, n-butane conversion is approximately 82～85%.The variation that temperature of molten salt is small can cause the bigger variation of reaction temperature, thereby has influence on conversion ratio and optionally variation, finally has influence on the yield of cis-butenedioic anhydride.
The high-temperature molten salt that flows through shell side in the reactor; A part of open degree through control valve or manually-operated gate; Control the fused salt flow of the fused salt cooler of flowing through; Cooled low-temperature molten salt mixes the shell side of back Returning reactor with the high-temperature molten salt of circulation, reach the control exothermic heat of reaction and shift out, realization response device shell side temperature of molten salt stable.
Adopt the open degree control method of control valve or manually-operated gate, the temperature of molten salt automatic or manual is regulated control, and the temperature of molten salt undulating value fluctuates reaction temperature at ± 2～3 ℃ thereupon, has influence on oxidation reaction selectivity and yield of maleic anhydride.
Control valve or hand-operated valve implement to regulate control
Control valve is opened precision 1%
Control valve open degree 1 degree
Automatic control output signal 4～20mA
The embodiment of the invention 1:
Working condition is identical with Comparative Examples:
When (shell side) temperature of molten salt departs from technological parameter controlling value (high or low) in the reactor; Regulate the electric operator 10 that control signal exports guiding valve to through DCS (Distributed Control System); Through connecting rod 19 control spools 18; The stroke aperture of regulating slide valve spool 18 moves up or down spool, changes high-temperature molten salt through the overlapping circulation area of opening on change and the valve seat 17 and exports 13 flows; Reach the fused salt flow of controlling the fused salt cooler of flowing through, realize the purpose of control reactor shell side temperature of molten salt.
The high-temperature molten salt that flows through shell side in the reactor; A part of through accurately controlling the open degree of guiding valve; Control the fused salt flow of the fused salt cooler of flowing through; Cooled low-temperature molten salt mixes the shell side of back Returning reactor with the high-temperature molten salt of circulation, reach the control exothermic heat of reaction and shift out, realization response device shell side temperature of molten salt stable.
Adopt the guiding valve accuracy control method, reach temperature of molten salt and regulate control automatically, solve and overcome reaction temperature and fluctuate, improve oxidation reaction selectivity and yield of maleic anhydride.
Guiding valve implements to regulate automatically control
In oxidation reaction process; Adopt said method to reach temperature of molten salt and regulate control automatically, through the open degree of accurate control guiding valve, realization response device shell side temperature of molten salt stable; Solve and overcome reaction temperature and fluctuate, improve oxidation reaction selectivity and yield of maleic anhydride.Its result of implementation sees the following form.
Temperature control contrast is as shown in Figure 5:
In oxidation reaction process; Adopt guiding valve adjustment control method of the present invention to reach temperature of molten salt and regulate control automatically; Open degree through accurate control guiding valve; Realization response device shell side temperature of molten salt stable solves and overcomes the reaction temperature fluctuation, make the reactor temperature of molten salt by former control ± 2～3 ℃ be accurate to ± 0.5 ℃ of scope.Improve oxidation reaction selectivity and yield of maleic anhydride, make oxidation reaction cis-butenedioic anhydride weight yield improve 0.5～1.0%, cis-butenedioic anhydride product promptly per ton reduces raw material (normal butane) and consumes 12～14kg.Simultaneously, improve the selectivity of oxidation reaction, reduced the accessory substance in the reaction product.
Claims (6)
1. a normal butane method fixed bed cis-butenedioic anhydride is produced the oxidizing reaction temperature control set for adjusting; It is characterized in that between reactor (1) and fused salt cooler (2), being provided with guiding valve (10); Circuit is connected under the fused salt of the high-temperature molten salt of guiding valve inlet (12) and reactor; High-temperature molten salt outlet (13) is connected with the high-temperature molten salt inlet of fused salt cooler (2), and low-temperature molten salt return port (20) is connected with the fused salt cocircuit that fused salt refluxing opening (14) is connected fused salt cooler and reactor.
2. device as claimed in claim 1 is characterized in that described guiding valve comprises valve body (15), expansion joint (16), valve seat (17), spool (18) and connecting rod (19); Be provided with expansion joint (16) in the middle of the valve body, connecting rod connects spool and the auto-controlled electric executing agency (10) above the valve body in valve body, and valve seat is provided with the opening corresponding with spool (21).
3. device as claimed in claim 2 is characterized in that valve seat (17) is the sleeve that is fixed in the valve body, and the position is in the high-temperature molten salt porch, and enters the mouth greater than high-temperature molten salt; Around sleeve, be provided with uniform opening (21); In valve seat, be provided with spool, spool is the sleeve that loam cake is arranged, and highly is 2 times of valve seat; The loam cake of spool connects connecting rod (19); Be provided with one deck baffle plate in the middle of the valve cage, the opening position corresponding with valve seat is provided with spool bore (18) on the sleeve below the baffle plate, and the area of spool bore is less than the area of opening; Valve seat is that piston is connected with spool.
4. device as claimed in claim 3 is characterized in that described via count is 4～8.
5. device as claimed in claim 3 is characterized in that described spool bore is the hole that meets the arbitrary shape of linear circulation.
6. device as claimed in claim 3 is characterized in that described spool bore is trapezoidal, taper or triangle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120300026XU CN202185300U (en) | 2011-08-18 | 2011-08-18 | Device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in fixed bed by normal butane method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201120300026XU CN202185300U (en) | 2011-08-18 | 2011-08-18 | Device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in fixed bed by normal butane method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202185300U true CN202185300U (en) | 2012-04-11 |
Family
ID=45916779
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201120300026XU Expired - Lifetime CN202185300U (en) | 2011-08-18 | 2011-08-18 | Device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in fixed bed by normal butane method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202185300U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102423666A (en) * | 2011-08-18 | 2012-04-25 | 天津市化工设计院 | Oxidation reaction temperature regulation control device and method in fixed bed maleic anhydride production with normal butane method |
| CN103537243A (en) * | 2013-10-30 | 2014-01-29 | 天津市化工设计院 | Device and method for removing reaction heat in acrolein oxidation |
| CN104242456A (en) * | 2014-09-26 | 2014-12-24 | 国家电网公司 | Feeder automation method and feeder automation system for power distribution network |
-
2011
- 2011-08-18 CN CN201120300026XU patent/CN202185300U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102423666A (en) * | 2011-08-18 | 2012-04-25 | 天津市化工设计院 | Oxidation reaction temperature regulation control device and method in fixed bed maleic anhydride production with normal butane method |
| CN102423666B (en) * | 2011-08-18 | 2013-07-17 | 天津市化工设计院 | Oxidation reaction temperature regulation control device and method in fixed bed maleic anhydride production with normal butane method |
| CN103537243A (en) * | 2013-10-30 | 2014-01-29 | 天津市化工设计院 | Device and method for removing reaction heat in acrolein oxidation |
| CN103537243B (en) * | 2013-10-30 | 2015-11-11 | 天津市化工设计院 | Acrolein oxidation reaction heat moving-out device and method |
| CN104242456A (en) * | 2014-09-26 | 2014-12-24 | 国家电网公司 | Feeder automation method and feeder automation system for power distribution network |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102423666B (en) | Oxidation reaction temperature regulation control device and method in fixed bed maleic anhydride production with normal butane method | |
| CN202185300U (en) | Device for adjusting and controlling temperature of oxidizing reaction in maleic anhydride production in fixed bed by normal butane method | |
| CN103977796B (en) | Catalyst used in preparation of long-chain alkane through catalytic hydrodeoxygenation of biomass | |
| CN109400443B (en) | Device and method for preparing ethylene glycol through dimethyl oxalate hydrogenation | |
| CN103769008B (en) | Slurry bed system common loop reactor | |
| CN101613289A (en) | The abbreviated system that thanomin is produced | |
| CN106076211A (en) | A kind of bubble-liquid two-phase jet reactor and bubble-liquid two-phase jet response system | |
| CN104176705B (en) | A kind of sulfur resistant conversion process of producing synthesis gas | |
| CN111217686A (en) | Preparation method of n-valeraldehyde and special Venturi ejector | |
| CN104262173B (en) | A kind of method of being synthesized diglycolamine by glycol ether low-pressure process | |
| CN112574157A (en) | Device and method for continuous liquid state alkyl passing in Grignard reaction | |
| CN105647657B (en) | A kind of biodiesel oil methyl esterizing device and its production technology | |
| CN104792921A (en) | Catalyst performance evaluation device and catalyst performance evaluation method | |
| CN112194566A (en) | Device and process for synthesizing methanol based on carbon dioxide hydrogenation | |
| CN207680578U (en) | A kind of fixed bed reactors suitable for gas phase exothermic reaction | |
| CN104150439A (en) | Carbon monoxide shifting process | |
| CN104672177B (en) | A kind of hexafluoropropylene oxide continuous production processes | |
| CN209109181U (en) | Diazinon cyclization reaction device | |
| CN103664671B (en) | Continuous production method of o-aminobenzoic acid | |
| CN101966472B (en) | Device for reducing catalyst for catalytic synthesis of dimethyl ether by one-step method | |
| CN201848255U (en) | Catalyst reduction device for one-step catalytic synthesis of dimethyl ether gas | |
| CN205258426U (en) | Preparation biodiesel's ester exchange tower cauldron formula consecutive reaction device | |
| CN103756716B (en) | Biomass-oil catalytic hydrogenation reaction device and catalytic hydrogenation method thereof | |
| CN104815593A (en) | Bubbling reactor and use thereof | |
| CN206215185U (en) | A kind of isothermal reactor for polymethoxy dimethyl ether synthesis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170227 Address after: 300457 Tianjin City Garden Villa Binhai New Area Development Zone No. 14 Patentee after: Bohai Tianjin chemical industry group planning and Design Institute Address before: 300193 Tianjin City, Nankai District Yangtze River Road, Gushan Road No. 2 Patentee before: Tianjin Chemical Design Inst. |
|
| CP03 | Change of name, title or address |
Address after: 300457 No. 2, Gushan Road, Changjiang Road, Tianjin, Nankai District Patentee after: Tianjin Bohai Chemical Engineering Co., Ltd. Address before: 300457 Tianjin City Garden Villa Binhai New Area Development Zone No. 14 Patentee before: Bohai Tianjin chemical industry group planning and Design Institute |
|
| CP03 | Change of name, title or address | ||
| CX01 | Expiry of patent term |
Granted publication date: 20120411 |
|
| CX01 | Expiry of patent term |