CN203408693U - Hydrogenation reactor taking acetic acid as raw material - Google Patents
Hydrogenation reactor taking acetic acid as raw material Download PDFInfo
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- CN203408693U CN203408693U CN201320487459.XU CN201320487459U CN203408693U CN 203408693 U CN203408693 U CN 203408693U CN 201320487459 U CN201320487459 U CN 201320487459U CN 203408693 U CN203408693 U CN 203408693U
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Abstract
The utility model relates to a hydrogenation reactor taking acetic acid as a raw material, and specifically relates to gas-solid phase reaction coupled fixed bed catalyst reactor. The reactor comprises an insulating reaction section and a tubular reaction section, wherein a mixed distributor which uniformly distributes hydrogen, acetic acid and ester steam thereof is arranged at a gas inlet of the reactor. The insulating reaction section is arranged above the tubular reaction section and is sequentially filled by a hydrogenation catalyst and an inertial fire-resistant ceramic ball from bottom to top. The hydrogenation catalyst is uniformly filled in a tube of the tubular reaction section. Compared with the prior art, the reactor provided by the utility model has the advantages of reasonable distribution of reactor temperature, high utilization ratio of a catalyst bed layer, convenience and uniformity in filling the catalyst and the like.
Description
Technical field
The utility model relates to a kind of reactor, is specifically related to a kind ofly for take the technical process that acetic acid and ester class series of products thereof are waste ethanol, and the gas of employing while carrying out hydrogenation is, the fixed bed catalytic reactor of solid phase reaction.
Background technology
Acetic acid is a kind of important industrial chemicals, mainly for the production of acetate, vinyl acetate, PTA etc.Acetic acid prior synthesizing method is mainly ethylene process and Ethanol Method, and cost is higher.Acetic acid synthetic technology innovation subsequently, carbonylation method becomes the market mainstream because cost is lower.In recent years China scientific research institution develop have independent intellectual property right based on carbonylation method Processes for Producing Acetic Acid, the domestic a collection of acetic acid plant that also in succession started, expansion along with acetic acid production capacity, China has become production of acetic acid the first big country, within 2011, acetic acid production capacity is approximately 6,700,000 tons, and demand is only 4,200,000 tons, within 2012, acetic acid production capacity is over 7,500,000 tons, expectation will break through 1,000 ten thousand tons acetic acid production capacity in 2015, acetic acid industry problem of excess production capacity is outstanding, the weakness of demand of acetic acid downstream, consumption still concentrates on traditional application, there is not significant change in consumption structure, also caused thus acetic acid price within long period of time, low level to be moved.Production capacity how to carry out balance surplus is acetic acid industry problem demanding prompt solution.
Ethanol is important industrial chemicals, and application is extensive, and ethanol, as a kind of good vehicle fuel, has also worldwide obtained and promoted and approval simultaneously, wherein particularly successful in the U.S. and Brazil, in China, gathers around and has broad application prospects.To alcohol fuel, there is huge potential consumption demand in China, but since 2009, country reduces year by year to the financial subsidies of fixed point grain method fuel ethanol production enterprise, non-grain method fuel ethanol production tallies with the national condition, for acetic acid and ester class series of products preparation of ethanol by hydrogenating thereof have brought the good market opportunity.
The reaction of acetic acid and ester class series of products preparation of ethanol by hydrogenating thereof adopts tubular reaction section conventionally, and such reactor batch temperature is even, easy to operate, byproduct steam, and energy is recycled rationally.But such reactor catalyst space-time yield is low, and beds epimere temperature is lower, bed epimere catalyst utilization is not high, cause reactor production capacity low, Catalyst packing difficulty easily causes Catalyst packing inhomogeneous in filling process, and catalyst is easily poisoning, affects service life.
Summary of the invention
The purpose of this utility model is exactly in order to overcome the defect that above-mentioned prior art exists, to provide a kind of to make that temperature of reactor distributes rationally, beds utilization rate is high, Catalyst packing convenient and acetic acid hydrogenation reactor uniformly.
The purpose of this utility model can be achieved through the following technical solutions: a kind of acetic acid hydrogenation reactor, coupling fixed bed catalytic reactor for gas-solid phase reaction, comprise an adiabatic reaction section and a pipe reaction section, it is characterized in that, in the gas feed of reactor, be provided with the equally distributed mixed distribution device of hydrogen and acetic acid and ester class steam thereof; Described adiabatic reaction section is arranged on pipe reaction section top, and adiabatic reaction section is loaded hydrogenation catalyst, inertia alumina ball from bottom to top successively, evenly loads hydrogenation catalyst in the pipe of pipe reaction section.
The amount of the hydrogenation catalyst of described adiabatic reaction section filling be the filling of pipe reaction section hydrogenation catalyst weight 5～30%.
The inertia alumina ball of described adiabatic reaction section filling comprises two kinds: size is that Φ 4～6mm inertia alumina ball is seated in above hydrogenation catalyst, loading height is 30～200mm, size is that Φ 10～20mm inertia alumina ball is seated in the superiors, and loading height is 50～300mm.
The internal diameter of the reactor tubulation of described pipe reaction section is Φ 30mm～50mm, and pipe range is 5000mm～8000mm.
The reactor shell top of described pipe reaction section is provided with heat transferring medium outlet, bottom is provided with heat transferring medium entrance, the conduction oil that heat exchange is used or boiler feed water flow into from heat transferring medium entrance, from heat transferring medium outlet, flow out, evenly shift out and on reaction tube Inner catalyst, carry out hydrogenation reaction institute liberated heat.
Described mixed distribution device is diffusion type or injecting type mixed distribution device.
Described pipe reaction section lower perforated plate is basic identical to structure and the conventional tubular reaction segment structure at gas-vapour material outlet place.
Compared with prior art, the utility model is at reactor inlet place, equally distributed diffusion type (or injecting type) mixed distribution device is set, simultaneously at the top of beds filling inertia alumina ball, reacting gas is uniformly distributed, prevent gas bias current, guarantee that in reactor, axially the load of beds is consistent everywhere; For reaction bed temperature is raise rapidly, reach the needed temperature of reaction, improve beds utilization rate, adiabatic reaction section is set on shell conversion zone, can also bring thus a benefit, this adiabatic reaction section can also effectively be avoided the impacts of poisonous substance on the shell conversion zone inner catalyst of main body such as sulphur, phosphorus, arsenic, chlorine, effectively improves the whole service life of catalyst; Upper perforated plate by shell conversion zone between adiabatic reaction section and shell conversion zone is directly cascaded, and during catalyst in filling shell conversion zone, can be undertaken by adiabatic reaction section, and filling operating surface is large, and efficiency is high, and it is even to be convenient to manage the filling of inner catalyst.
In the utility model, adiabatic reaction section and shell conversion zone are effectively coupled, and have advantages of that reacting gas is evenly distributed, bed temperature distributes rationally, production capacity is large, byproduct steam, energy recovery utilization rate is high, Catalyst packing is convenient, catalyst extends service life.
Accompanying drawing explanation
Fig. 1 is the structural representation of the coupling fixed bed reactor of the utility model;
Label in figure is respectively:
1, reacting gas inlet, 2, upper cover, 3, gas distributor, 4, inertia alumina ball layer a, 5, inertia alumina ball layer b, 6, adiabatic section bed, 7, upper perforated plate, 8, heat transferring medium outlet, 9, cylindrical shell, 10, reactor tubulation, 11, heat transferring medium import, 12, lower perforated plate, 13, low head, 14, reacting product outlet.
The specific embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is elaborated.
Embodiment
As shown in Figure 1, a kind of coupling fixed bed reactor, by the reactor urceolus 9, upper cover 2, the low head 13 that bear high pressure, form cylindrical shell, on upper cover 2, be provided with reaction gas inlet 1, gas distributor 3, on low head 13, be provided with product outlet 14, urceolus 9 is provided with heat transferring medium outlet 8, heat transferring medium import 11.
Inner barrel is divided three parts, first be hydrogen and acetic acid and the equally distributed diffusion type of ester class steam (or injecting type) mixed distribution device 3 thereof,
In cylindrical shell, second portion is adiabatic reaction section, adiabatic reaction section is arranged on pipe reaction section top, adiabatic reaction section is loaded the adiabatic section bed 6 of hydrogenation catalyst from bottom to top successively, the inertia alumina ball layer b5 of Φ 4mm～6mm, loading height is 30～200mm, the inertia alumina ball layer a4 of Φ 10mm～20mm, loading height is 50～300mm.
Cylindrical shell third part is pipe reaction section, comprises the heat transferring medium outside reactor tubulation 10 and reactor tubulation, and reactor tubulation 10 is arranged by equilateral triangle or concentric circles mode, uses card constant spacing between reaction tube.The full hydrogenation catalyst of the inner filling of reaction tube.Reactor tubulation 10 tops are provided with upper perforated plate 7, and bottom is provided with lower perforated plate 12.The internal diameter of reactor tubulation 10 is Φ 30mm～50mm, and pipe range is 5000mm～8000mm.The amount of the hydrogenation catalyst of described adiabatic reaction section filling be the filling of pipe reaction section hydrogenation catalyst weight 5～30%.
Raw hydrogen and acetic acid or its ester class steam enter reactor from reaction gas inlet 1, by entering again inertia alumina ball layer a4 and inertia alumina ball layer b5 after gas distributor 3, reacting gas is uniformly distributed, prevent gas bias current, enter subsequently the adiabatic section bed 6 of filling hydrogenation catalyst, at the interior gas raw material of this adiabatic section bed 6, heat up rapidly, reach and react temperature required and remove entering in the reactor tubulation 10 of pipe reaction section after the poisonous impurity component of catalyst, in beds, react.
Heat transferring medium (conduction oil or boiler feed water) enters shell-and-tube conversion zone from heat transferring medium import 11, leaves reactor after taking away the heat that shell-and-tube conversion zone hydrogenation reaction produces from heat transferring medium outlet 8, forms reaction bed Temperature Distribution.
It is more than preferred embodiment of the present utility model; for those skilled in the art; without departing from the concept of the premise utility, can also change this reactor subtlety, these changes also should be considered as in protection domain of the present utility model.
Claims (6)
1. an acetic acid hydrogenation reactor, coupling fixed bed catalytic reactor for gas-solid phase reaction, comprise an adiabatic reaction section and a pipe reaction section, it is characterized in that, in the gas feed of reactor, be provided with the equally distributed mixed distribution device of hydrogen and acetic acid and ester class steam thereof; Described adiabatic reaction section is arranged on pipe reaction section top, and adiabatic reaction section is loaded hydrogenation catalyst, inertia alumina ball from bottom to top successively, evenly loads hydrogenation catalyst in the pipe of pipe reaction section.
2. a kind of acetic acid hydrogenation reactor according to claim 1, is characterized in that, the amount of the hydrogenation catalyst of described adiabatic reaction section filling be the filling of pipe reaction section hydrogenation catalyst weight 5～30%.
3. a kind of acetic acid hydrogenation reactor according to claim 1, it is characterized in that, the inertia alumina ball of described adiabatic reaction section filling comprises two kinds: size is that Φ 4～6mm inertia alumina ball is seated in above hydrogenation catalyst, loading height is 30～200mm, size is that Φ 10～20mm inertia alumina ball is seated in the superiors, and loading height is 50～300mm.
4. a kind of acetic acid hydrogenation reactor according to claim 1, is characterized in that, the internal diameter of the reactor tubulation of described pipe reaction section is Φ 30mm～50mm, and pipe range is 5000mm～8000mm.
5. a kind of acetic acid hydrogenation reactor according to claim 1, it is characterized in that, the reactor shell top of described pipe reaction section is provided with heat transferring medium outlet, bottom is provided with heat transferring medium entrance, the conduction oil that heat exchange is used or boiler feed water flow into from heat transferring medium entrance, from heat transferring medium outlet, flow out, evenly shift out and on reaction tube Inner catalyst, carry out hydrogenation reaction institute liberated heat.
6. a kind of acetic acid hydrogenation reactor according to claim 1, is characterized in that, described mixed distribution device is diffusion type or injecting type mixed distribution device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320487459.XU CN203408693U (en) | 2013-08-09 | 2013-08-09 | Hydrogenation reactor taking acetic acid as raw material |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320487459.XU CN203408693U (en) | 2013-08-09 | 2013-08-09 | Hydrogenation reactor taking acetic acid as raw material |
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| CN203408693U true CN203408693U (en) | 2014-01-29 |
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| CN201320487459.XU Expired - Lifetime CN203408693U (en) | 2013-08-09 | 2013-08-09 | Hydrogenation reactor taking acetic acid as raw material |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104857894A (en) * | 2015-05-04 | 2015-08-26 | 河南顺达化工科技有限公司 | Ethanol synthesis reactor with heat exchange unit |
| CN106179132A (en) * | 2016-08-30 | 2016-12-07 | 凯瑞环保科技股份有限公司 | A kind of mixing carbon four selectivity for high concentration alkynes and alkadienes is hydrogenated with calandria type fixed bed reactor altogether |
| CN107262009A (en) * | 2017-06-22 | 2017-10-20 | 北京科田高新技术有限公司 | A kind of novel reactor and its application in production polyarylether |
| CN108371876A (en) * | 2018-04-03 | 2018-08-07 | 青岛华世洁环保科技有限公司 | A kind of catalytic oxidizing equipment and method of efficient process VOCs organic exhaust gas |
| CN109395668A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of coupled reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN110624480A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Fixed bed reactor and unsaturated light hydrocarbon hydrogenation method |
| CN113856569A (en) * | 2021-09-28 | 2021-12-31 | 联化新瑞(北京)科技有限公司 | Reactor for preparing succinic anhydride through maleic anhydride hydrogenation and control method thereof |
| CN113856568A (en) * | 2021-09-28 | 2021-12-31 | 联化新瑞(北京)科技有限公司 | Reactor for preparing 1, 3-propylene glycol by hydrogenating 3-hydroxypropionaldehyde and control method thereof |
-
2013
- 2013-08-09 CN CN201320487459.XU patent/CN203408693U/en not_active Expired - Lifetime
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104857894A (en) * | 2015-05-04 | 2015-08-26 | 河南顺达化工科技有限公司 | Ethanol synthesis reactor with heat exchange unit |
| CN106179132A (en) * | 2016-08-30 | 2016-12-07 | 凯瑞环保科技股份有限公司 | A kind of mixing carbon four selectivity for high concentration alkynes and alkadienes is hydrogenated with calandria type fixed bed reactor altogether |
| CN107262009A (en) * | 2017-06-22 | 2017-10-20 | 北京科田高新技术有限公司 | A kind of novel reactor and its application in production polyarylether |
| CN109395668A (en) * | 2017-08-18 | 2019-03-01 | 上海浦景化工技术股份有限公司 | A kind of coupled reactor for oxalic acid Arrcostab hydrogenation synthesizing of ethylene glycol |
| CN108371876A (en) * | 2018-04-03 | 2018-08-07 | 青岛华世洁环保科技有限公司 | A kind of catalytic oxidizing equipment and method of efficient process VOCs organic exhaust gas |
| CN108371876B (en) * | 2018-04-03 | 2024-03-22 | 青岛华世洁环保科技有限公司 | Catalytic oxidation device and method for efficiently treating VOCs organic waste gas |
| CN110624480A (en) * | 2018-06-22 | 2019-12-31 | 中国石油化工股份有限公司 | Fixed bed reactor and unsaturated light hydrocarbon hydrogenation method |
| CN110624480B (en) * | 2018-06-22 | 2022-07-12 | 中国石油化工股份有限公司 | Fixed bed reactor and unsaturated light hydrocarbon hydrogenation method |
| CN113856569A (en) * | 2021-09-28 | 2021-12-31 | 联化新瑞(北京)科技有限公司 | Reactor for preparing succinic anhydride through maleic anhydride hydrogenation and control method thereof |
| CN113856568A (en) * | 2021-09-28 | 2021-12-31 | 联化新瑞(北京)科技有限公司 | Reactor for preparing 1, 3-propylene glycol by hydrogenating 3-hydroxypropionaldehyde and control method thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANGHAI PUJING CHEMICAL INDUSTRY TECHNOLOGY CO., Free format text: FORMER NAME: PUJING CHEMICAL INDUSTRY (SHA) LIMITED |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 201600 Zhongshan Songjiang District Road, No. 62, building eleventh, room 1, Building 102 Patentee after: PUJING CHEMICAL INDUSTRY Co.,Ltd. Address before: 201600 Zhongshan Songjiang District Road, No. 62, building eleventh, room 1, Building 102 Patentee before: Pujing Chemical Industry (Shanghai) Ltd. |
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| CX01 | Expiry of patent term |
Granted publication date: 20140129 |
|
| CX01 | Expiry of patent term |