CN2621805Y - Shell external cooling-thermal insulating and combined fixed bed catalyst chember - Google Patents
Shell external cooling-thermal insulating and combined fixed bed catalyst chember Download PDFInfo
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- CN2621805Y CN2621805Y CN 03231767 CN03231767U CN2621805Y CN 2621805 Y CN2621805 Y CN 2621805Y CN 03231767 CN03231767 CN 03231767 CN 03231767 U CN03231767 U CN 03231767U CN 2621805 Y CN2621805 Y CN 2621805Y
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Abstract
The utility model is an adiabatic-tube-shell type fixed bed catalyst chamber, which comprises at least an adiabatic reaction zone and a shell reaction zone which are mutually-connected in series. The utility model combines the advantages of tube shell reactor and adiabatic reactor, and has the advantages of large production capability, high recovery and reused rate of power, by-product steam, reasonable bed temperature, extended service life of catalyst and so on. The utility model is applicable to the reaction process of methanol synthesis, ammonia synthesis, carbon monoxide conversion, hydrogenation of organic compounds, dimethyl ether synthesis, ethylene oxide synthesis, and other reversible exothermic reaction processes. The utility model is suitable for new device as well as for the capability-expansion of original production facilities.
Description
Technical field
The utility model relates to a kind of reactor, is specifically related to a kind of gas solid phase fixed bed catalyst chamber.
Background technology
Solid catalyst is used in most of Industrial Catalysis reactions, and the reactor that uses is gas solid catalytic reactor.Fixed bed catalytic reactor is an equipment commonly used in the chemical industry, and, ammonia synthesis, carbon monodixe conversion, organic compound hydrogenation synthetic at methyl alcohol, dimethyl ether is synthetic, oxirane is synthetic, be used widely in other reversible exothermic catalytic reactions.Fixed bed catalytic reactor can be divided into heat-insulating and Continuous Heat Transfer formula by heat exchange mode.Multistage insulation formula catalytic reactor can be divided into direct cold shock formula and indirect heat exchange formula, and Continuous Heat Transfer formula catalytic reactor can be divided into external-cooling type and inner-cooled.External-cooling type catalytic reactor, catalyst are seated in the pipe, and pipe is outer to be heat transferring medium, so the external-cooling type catalytic reactor also claims the shell of pipe exterior formula.For the inner-cooled catalytic reactor, catalyst is seated between pipe, is unreacted gas in the pipe.
Shell of pipe exterior formula catalytic reactor, as German Lurgi shell-and-tube reactor (patent DE2123950), Japanese excess revolutions reactor (patent JP63-123433).Such reactor catalysis bed temperature is steady, easy to operate, recovers energy rationally.But also there is significant disadvantages in this reactor, and single tower production capacity is low, and there is serious wall effect in the reactor catalysis bed, influences the catalyst space-time yield, and catalyst easily poisons, and influences service life.
The intersegmental cold shock formula of multistage insulation reactor, as Britain ICI multistage cold shock reactor (the room ancient cooking vessel already waits and writes, methanol production technology and progress, Shanghai: Huadong Chemical College publishing house, 1990), multistage is adiabatic reaction, the intersegmental thermal recovery unstripped gas cold shock mode of moving.Such reactor production capacity is big, simple in structure, easy to manufacture, but the catalytic bed temperature distribution is not ideal enough, and reactor operation and temperature control difficulty are big, and gas backmixing is serious, and conversion ratio is low, and energy utilizes unreasonable.
The intersegmental indirect heat exchange formula of multistage insulation reactor, (the room ancient cooking vessel already waits and writes as Tops φ e Radial Flow adiabatic reactor, methanol production technology and progress, Shanghai: Huadong Chemical College publishing house, 1990), reaction system is made up of the Radial Flow reactor of three adiabatic operations, between three reactors external heat exchanger is set and removes reaction heat.Such gas reactor Radial Flow, pressure falls little, the catalyst utilization height, production capacity is big, recover energy rationally, but equipment investment is bigger, and reactor is made complicated, and catalytic bed temperature distributes not ideal enough.
Summary of the invention
The utility model technical issues that need to address are a kind of outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation of design, to overcome the above-mentioned defective that prior art exists, adapt to the requirement of large scale development, make that temperature of reactor distributes rationally, operation control is easy, energy recovery rate is high.
Design of the present utility model is such: the said reactor of the utility model comprises adiabatic reaction section and the shell conversion zone that is connected in series at least.Reaction is mainly in the shell section, at the shell conversion zone, pass through tube wall, heat is passed to the boiled water of shell side, under the situation near isothermal, gas is from top to down by catalytic bed, and catalytic reaction and catalytic bed are conducted heat to the shell side boiled water and carried out simultaneously, in time heat is emitted in reaction and pass to boiled water, byproduct steam.
According to above-mentioned design, the inventor has proposed following technical scheme:
A kind of outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation comprises an adiabatic reaction section and a shell conversion zone of being connected in series mutually at least;
Said adiabatic reaction section comprises adiabatic section cylindrical shell, adiabatic section reaction gas inlet and the outlet of adiabatic section reaction gas, catalyst is seated in the cylindrical shell of adiabatic section, the adiabatic section reaction gas inlet is arranged on the adiabatic section cylinder top, and reaction gas outlet in adiabatic section is arranged on cylindrical shell bottom, adiabatic section;
Said shell conversion zone comprises shell section cylindrical shell, upper perforated plate, lower perforated plate, tubulation, water inlet, steam (vapor) outlet, shell section reaction gas inlet and the outlet of shell section reaction gas, tubulation is fixed on the lower perforated plate, catalyst is seated in the tubulation, shell section raw material gas inlet is arranged on shell section cylindrical shell upper end, the outlet of shell section reaction gas is arranged on shell section cylindrical shell lower end, and water inlet, steam (vapor) outlet are arranged on the shell conversion zone cylindrical shell and with the cavity of shell side in the shell conversion zone cylindrical shell and communicate.
The utility model combines the advantage of shell of pipe exterior and adiabatic reactor, have that production capacity is big, energy recovery utilization rate height, byproduct steam, bed temperature rationally, the advantage that prolongs service life of catalyst: 1. adapt to the maximization process units, as be suitable for producing per year the production scale of 600,000 tons, 900,000 tons methyl alcohol; 2. effectively utilize reaction heat, the steam of by-product 1～4Mpa; 3. Temperature Distribution is reasonable, and unstripped gas utilizes adiabatic reaction to improve the reaction gas temperature in the leading portion adiabatic reactor, near entering shell section reactor after the optimum temperature; 4. improve reaction-ure conversion-age, in the back segment adiabatic reactor, the reactant of low concentration reacts again, further improves conversion ratio; 5. improve the catalyst space-time yield; 6. catalyst prolongs service life.The utility model can be used for that methyl alcohol is synthetic, ammonia synthesis, carbon monodixe conversion, organic compound hydrogenation, dimethyl ether is synthetic, oxirane is synthetic, other reversible exothermic reaction processes.The utility model both had been suitable for new device, also was fit to original production device capacity expansion revamping.
Description of drawings
Fig. 1 is arranged on the outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation schematic diagram on shell conversion zone top for the adiabatic reaction section.
Fig. 2 is arranged on the outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation schematic diagram on shell conversion zone top for the adiabatic reaction section of another kind of form.
Fig. 3 is arranged on the outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation schematic diagram of shell conversion zone bottom for the adiabatic reaction section.
Fig. 4 is arranged on the outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation schematic diagram of shell conversion zone bottom for the adiabatic reaction section of another kind of form.
Fig. 5 is the outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation schematic diagram that is provided with two adiabatic reaction sections.
Fig. 6 is the outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation schematic diagram that is provided with two adiabatic reaction sections of another kind of form.
The specific embodiment
Referring to Fig. 1, outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation of the present utility model comprises an adiabatic reaction section 1 and a shell conversion zone 2 of being connected in series mutually;
Said adiabatic reaction section 1 comprises adiabatic section cylindrical shell 101, adiabatic section reaction gas inlet 102 and adiabatic section reaction gas outlet 103, catalyst is seated in the adiabatic section cylindrical shell 101, adiabatic section reaction gas inlet 102 is arranged on adiabatic section cylindrical shell 101 tops, and adiabatic reaction gas outlet 103 is arranged on adiabatic section cylindrical shell 101 bottoms;
Said shell conversion zone 2 comprises shell section cylindrical shell 201, upper perforated plate 202, lower perforated plate 203, tubulation 204, water inlet 205, steam (vapor) outlet 206, shell section reaction gas inlet 207 and shell section reaction gas outlet 208, tubulation 204 is fixed on, lower perforated plate 202, on 203, catalyst is seated in the tubulation 204, shell section reaction gas inlet 207 is arranged on shell section cylindrical shell 201 upper ends, shell section reaction gas outlet 208 is arranged on shell section cylindrical shell 201 lower ends, water inlet 205, steam (vapor) outlet 206 is arranged on the shell conversion zone cylindrical shell 201 and with the cavity of shell side in the shell conversion zone cylindrical shell and communicates.Adiabatic reaction section 1 is arranged on shell conversion zone 2 tops, and adiabatic section reaction gas outlet 103 is connected with shell section reaction gas inlet 207.
The outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation of said structure is applicable to the situation that contains a certain amount of toxic component in the lower and unstripped gas of reactor feed gas temperature, can make unstripped gas reach the reaction preferred temperature in the adiabatic reaction section, improve outside the reaction efficiency, the effect of adsorbing the elimination poisonous substance in addition, prolong the service life of shell section catalyst, improve production intensity.
Referring to Fig. 2, its basic structure is identical with Fig. 1, and adiabatic reaction gas outlet 103 is connected by pipeline 3 with shell section raw material gas inlet 207.
Referring to Fig. 3, adiabatic reaction section 1 is identical with Fig. 1 with shell conversion zone 2 structures, it is characterized in that, adiabatic reaction section 1 is arranged on shell conversion zone 2 bottoms, and shell section reaction gas outlet 208 is connected with adiabatic section reaction gas inlet 102.The outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation of said structure is applicable to the situation that toxic component content in the higher and unstripped gas of reactor feed gas temperature is lower and need to obtain higher reaction efficiency.
Referring to Fig. 4, basic structure is identical with Fig. 3, it is characterized in that, shell section reaction gas outlet 208 is connected by pipeline 3 with the import 102 of adiabatic reaction gas.
Referring to Fig. 5, basic structure is identical with Fig. 1, it is characterized in that, shell conversion zone 2 bottoms are provided with an adiabatic reaction section 1 again, and shell section reaction gas outlet 208 is connected with the adiabatic reaction gas import 102 of this adiabatic reaction section 1.
Referring to Fig. 6, basic structure is identical with embodiment shown in Figure 2, it is characterized in that, shell conversion zone 2 bottoms are provided with an adiabatic reaction section 1 again, and shell section reaction gas outlet 208 is connected by pipeline 3 with the adiabatic reaction gas import 102 of this adiabatic reaction section 1.
Claims (7)
1. an outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation is characterized in that, comprises the adiabatic reaction section (1) and the shell conversion zone (2) that are connected in series mutually at least;
Said adiabatic reaction section (1) comprises adiabatic section cylindrical shell (101), adiabatic section reaction gas inlet (102) and adiabatic section reaction gas outlet (103), catalyst is seated in the adiabatic section cylindrical shell (101), adiabatic section reaction gas inlet (102) is arranged on adiabatic section cylindrical shell (101) top, and adiabatic section reaction gas outlet (103) is arranged on adiabatic section cylindrical shell (101) bottom;
Said shell conversion zone (2) comprises shell section cylindrical shell (201), upper perforated plate (202), lower perforated plate (203), tubulation (204), water inlet (205), steam (vapor) outlet (206), shell section reaction gas inlet (207) and shell section reaction gas outlet (208), tubulation (204) is fixed on, lower perforated plate (202,203) on, catalyst is seated in the tubulation (204), shell section reaction gas inlet (207) is arranged on shell section cylindrical shell (201) upper end, shell section reaction gas outlet (208) is arranged on shell section cylindrical shell (201) lower end, water inlet (205), steam (vapor) outlet (206) is arranged on shell conversion zone cylindrical shell (201) and upward and with the cavity of shell side in the shell conversion zone cylindrical shell communicates.
2. outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation according to claim 1, it is characterized in that, adiabatic reaction section (1) is arranged on shell conversion zone (2) top, and adiabatic section reaction gas outlet (103) is connected with shell section reaction gas inlet (207).
3. outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation according to claim 1, it is characterized in that, adiabatic reaction section (1) is arranged on shell conversion zone (2) top, and adiabatic section reaction gas outlet (103) is connected by pipeline (3) with shell section reaction gas inlet (207).
4. outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation according to claim 1, it is characterized in that, adiabatic reaction section (1) is arranged on shell conversion zone (2) bottom, and shell section reaction gas outlet (208) is connected with adiabatic section reaction gas inlet (102).
5. outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation according to claim 1, it is characterized in that, adiabatic reaction section (1) is arranged on shell conversion zone (2) bottom, and shell section reaction gas outlet (208) is connected by pipeline (3) with adiabatic section reaction gas inlet (102).
6. outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation according to claim 2, it is characterized in that, shell conversion zone (2) bottom is provided with an adiabatic reaction section (1) again, and shell section reaction gas outlet (208) is connected with the adiabatic section reaction gas inlet (102) of this adiabatic reaction section (1).
7. outside cold package-Hybrid fixed bed catalytic reactor of thermal insulation according to claim 3, it is characterized in that, shell conversion zone (2) bottom is provided with an adiabatic reaction section (1) again, and shell section reaction gas outlet (208) is connected by pipeline (3) with the adiabatic section reaction gas inlet (102) of this adiabatic reaction section (1).
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| Application Number | Priority Date | Filing Date | Title |
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| CN 03231767 CN2621805Y (en) | 2003-06-03 | 2003-06-03 | Shell external cooling-thermal insulating and combined fixed bed catalyst chember |
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| CN 03231767 CN2621805Y (en) | 2003-06-03 | 2003-06-03 | Shell external cooling-thermal insulating and combined fixed bed catalyst chember |
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Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1310862C (en) * | 2005-04-30 | 2007-04-18 | 四川天一科技股份有限公司 | Synthetic tower for methanol |
| CN101058534B (en) * | 2006-04-18 | 2011-01-12 | 杭州林达化工技术工程有限公司 | Device and method for preparing dimethyl ether from methanol |
| CN101274879B (en) * | 2007-03-30 | 2011-08-10 | 中国石油化工股份有限公司 | Fluidizer for producing dimethyl ether by methanol dehydration |
| CN102649740A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing oxalate through CO catalytic coupling reaction |
| CN102649570A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for oxidative dehydrogenation of CO gas through catalytic reaction |
| CN102649696A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method of preparing ethylene glycol through oxalate gas phase catalytic hydrogenation |
| CN102649741A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing oxalic ester by carbon monoxide gaseous phase catalytic coupling reaction |
| CN102649709A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing ethylene glycol by gas-phase catalytically hydrogenating oxalate raw material |
| CN102649563A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for dehydrogenation through catalytic oxidation of carbon monoxide gas |
| CN102649564A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for dehydrogenating CO-containing mixed gas raw material by means of catalytic oxidation reaction |
| CN102649734A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for producing oxalate through catalytic coupling reaction of carbon monoxide |
| CN102649708A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for producing ethylene glycol through high-efficiency catalytic reaction of oxalate |
| CN102649562A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for dehydrogenation of CO gas raw material in virtue of catalytic oxidation |
| CN103813852A (en) * | 2011-09-23 | 2014-05-21 | 乔治洛德方法研究和开发液化空气有限公司 | Cooled reactor for production of dimethyl ether from methanol |
| CN105854737A (en) * | 2016-05-27 | 2016-08-17 | 合肥海川石化设备有限公司 | Synthesis tower for preparing mixed alcohols from biomass syngas |
| WO2018096018A1 (en) * | 2016-11-24 | 2018-05-31 | Haldor Topsøe A/S | Multi bed reactor comprising an adiabatic and a heated catalyst bed |
| CN109482128A (en) * | 2019-01-18 | 2019-03-19 | 山东诺为制药流体系统有限公司 | A kind of multi-thread reactor |
-
2003
- 2003-06-03 CN CN 03231767 patent/CN2621805Y/en not_active Expired - Lifetime
Cited By (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1310862C (en) * | 2005-04-30 | 2007-04-18 | 四川天一科技股份有限公司 | Synthetic tower for methanol |
| CN101058534B (en) * | 2006-04-18 | 2011-01-12 | 杭州林达化工技术工程有限公司 | Device and method for preparing dimethyl ether from methanol |
| CN101274879B (en) * | 2007-03-30 | 2011-08-10 | 中国石油化工股份有限公司 | Fluidizer for producing dimethyl ether by methanol dehydration |
| CN102649562A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for dehydrogenation of CO gas raw material in virtue of catalytic oxidation |
| CN102649564B (en) * | 2011-02-25 | 2014-07-02 | 中国石油化工股份有限公司 | Method for dehydrogenating CO-containing mixed gas raw material by means of catalytic oxidation reaction |
| CN102649696A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method of preparing ethylene glycol through oxalate gas phase catalytic hydrogenation |
| CN102649741A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing oxalic ester by carbon monoxide gaseous phase catalytic coupling reaction |
| CN102649709A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing ethylene glycol by gas-phase catalytically hydrogenating oxalate raw material |
| CN102649563A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for dehydrogenation through catalytic oxidation of carbon monoxide gas |
| CN102649564A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for dehydrogenating CO-containing mixed gas raw material by means of catalytic oxidation reaction |
| CN102649734A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for producing oxalate through catalytic coupling reaction of carbon monoxide |
| CN102649708A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for producing ethylene glycol through high-efficiency catalytic reaction of oxalate |
| CN102649740A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for preparing oxalate through CO catalytic coupling reaction |
| CN102649708B (en) * | 2011-02-25 | 2014-08-13 | 中国石油化工股份有限公司 | Method for producing ethylene glycol through high-efficiency catalytic reaction of oxalate |
| CN102649570A (en) * | 2011-02-25 | 2012-08-29 | 中国石油化工股份有限公司 | Method for oxidative dehydrogenation of CO gas through catalytic reaction |
| CN102649709B (en) * | 2011-02-25 | 2014-07-02 | 中国石油化工股份有限公司 | Method for preparing ethylene glycol by gas-phase catalytically hydrogenating oxalate raw material |
| CN102649696B (en) * | 2011-02-25 | 2014-07-02 | 中国石油化工股份有限公司 | Method of preparing ethylene glycol through oxalate gas phase catalytic hydrogenation |
| CN102649734B (en) * | 2011-02-25 | 2014-07-02 | 中国石油化工股份有限公司 | Method for producing oxalate through catalytic coupling reaction of carbon monoxide |
| CN102649563B (en) * | 2011-02-25 | 2014-07-23 | 中国石油化工股份有限公司 | Method for dehydrogenation through catalytic oxidation of carbon monoxide gas |
| CN102649740B (en) * | 2011-02-25 | 2014-07-23 | 中国石油化工股份有限公司 | Method for preparing oxalate through CO catalytic coupling reaction |
| CN102649562B (en) * | 2011-02-25 | 2014-07-23 | 中国石油化工股份有限公司 | Method for dehydrogenation of CO gas raw material in virtue of catalytic oxidation |
| CN103813852A (en) * | 2011-09-23 | 2014-05-21 | 乔治洛德方法研究和开发液化空气有限公司 | Cooled reactor for production of dimethyl ether from methanol |
| CN105854737A (en) * | 2016-05-27 | 2016-08-17 | 合肥海川石化设备有限公司 | Synthesis tower for preparing mixed alcohols from biomass syngas |
| WO2018096018A1 (en) * | 2016-11-24 | 2018-05-31 | Haldor Topsøe A/S | Multi bed reactor comprising an adiabatic and a heated catalyst bed |
| CN109482128A (en) * | 2019-01-18 | 2019-03-19 | 山东诺为制药流体系统有限公司 | A kind of multi-thread reactor |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Shanxi coke group Yida chemical Limited by Share Ltd Assignor: East China University of Science and Technology Contract fulfillment period: 2008.2.14 to 2011.2.14 Contract record no.: 2008310000003 Denomination of utility model: Shell external cooling-thermal insulating and combined fixed bed catalyst chember Granted publication date: 20040630 License type: General permission Record date: 20080529 |
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Free format text: COMMON LICENCE; TIME LIMIT OF IMPLEMENTING CONTACT: 2008.2.14 TO 2011.2.14 Name of requester: YIDA CHEMICAL CO., LTD., SHANXI COKE GROUP Effective date: 20080529 |
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| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: CHONGQING WANSHENG COAL CO., LTD. Assignor: East China University of Science and Technology Contract fulfillment period: 2008.8.29 to 2011.8.29 Contract record no.: 2008310000215 Denomination of utility model: Shell and shell cold and heat insulation compound fixed bed catalytic reactor Granted publication date: 20040630 License type: General permission Record date: 20081114 Assignee: Donghua Engineering Science & Technology Co., Ltd. Assignor: East China University of Science and Technology Contract fulfillment period: 2008.2.25 to 2011.2.25 Contract record no.: 2008310000223 Denomination of utility model: Shell and shell cold and heat insulation compound fixed bed catalytic reactor Granted publication date: 20040630 License type: General permission Record date: 20081119 |
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Free format text: COMMON LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2008.2.25 TO 2011.2.25; CHANGE OF CONTRACT Name of requester: DONGHUA ENGINEERING TECHNOLOGY CO., LTD. Effective date: 20081119 Free format text: COMMON LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2008.8.29 TO 2011.8.29; CHANGE OF CONTRACT Name of requester: CHONGQING WANSHENG COAL CO.,LTD. Effective date: 20081114 |
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Assignee: Erdos Guotai Chemical Co., Ltd. Assignor: East China University of Science and Technology Contract fulfillment period: 2009.4.15 to 2012.4.15 Contract record no.: 2009310000068 Denomination of utility model: Shell external cooling-thermal insulating and combined fixed bed catalyst chember Granted publication date: 20040630 License type: General permission Record date: 20090513 |
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Assignee: Erdos northwest Energy Chemical Co., Ltd. Assignor: East China University of Science and Technology Contract fulfillment period: 2009.3.26 to 2012.3.31 Contract record no.: 2009310000148 Denomination of utility model: Shell external cooling-thermal insulating and combined fixed bed catalyst chember Granted publication date: 20040630 License type: General permission Record date: 20090804 |
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Assignee: ANHUI ANQING SHUGUANG CHEMICAL (GROUP) CO., LTD. Assignor: East China University of Science and Technology Contract record no.: 2012310000084 Denomination of utility model: Shell external cooling-thermal insulating and combined fixed bed catalyst chember Granted publication date: 20040630 License type: Common License Record date: 20120611 |
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