CN1042664A - Catalytic distillation novel device and antigravity system - Google Patents
Catalytic distillation novel device and antigravity system Download PDFInfo
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- CN1042664A CN1042664A CN 88109705 CN88109705A CN1042664A CN 1042664 A CN1042664 A CN 1042664A CN 88109705 CN88109705 CN 88109705 CN 88109705 A CN88109705 A CN 88109705A CN 1042664 A CN1042664 A CN 1042664A
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Abstract
The present invention is characterized in that as a kind of catalytic distillation device conversion zone is divided into several beds, establishes a plate between two beds.Catalyst is not to fill in the tower after the Web materials with conventional method is packaged into parcel, but directly fills in form in bulk in the beds of conversion zone, and catalyst can directly be packed into by loading port, and used catalyst can directly draw off from unloading outlet.Operate simple and easyly, raise the efficiency, overcome the trouble that needs the workman enter filling in the tower or draw off the catalyst parcel.Because reactant directly contacts with catalyst, help the carrying out that react, improved the efficient of catalyst.
Description
The invention belongs to the novel device and a kind of new catalyst packing method that is used for this equipment of the catalytic distillation technology of chemical industry.
Technical background:
People are known, the catalytic distillation device is a catalytic reaction and separate the device that two processes are carried out in same equipment simultaneously, simplified flow process, and it is different with the product boiling point based on reactant, when reaction is carried out, make product and reactants separate,, make to react completely to destroy the balance of reaction.Because reaction heat is absorbed by material vaporization, not only can make reaction heat obtain utilizing, and can make to be reflected at and carry out the heat-obtaining equipment that must not assist under the steady temperature.
Carry out simultaneously for making reaction and separation energy, make vapour phase that upwards flows and the liquid phase that flows downward to pass the conversion zone at catalytic distillation tower middle part simultaneously, in the patent documentation of having delivered, the downspout that catalyst is placed board-like tower tray that has, as a subsidiary reaction bed, as U.S.Pat.3.634.534, its catalyst filling is restricted; Have catalyst packing in stainless steel cloth, as U.S.Pat.4.471.154, make several square members, the member of making other shapes that also has is distributed on the distillation tray, when making reactant flow through tower tray, diffuse in the catalyst mesh bag, under catalyst action, react; What also have uses glass wool cloth as U.S.Pat.4 215.011, adds the parcel that stainless steel cloth is bundled into, and places conversion zone, leaves the space between the parcel, makes vapour-liquid two convection current of being on good terms pass conversion zone.Above-mentioned various structural shape, complex structure, the cost height, drawing off of the filling of raw catelyst and used catalyst is all very miscellaneous, needs the workman to enter in the tower and operates.Because catalyst packing is in parcel, reactant will be diffused in the parcel and react through diffusion process; Product also will diffuse out in by parcel through diffusion process, the carrying out of influence reaction.
The purpose of invention:
The present invention has overcome above-mentioned shortcoming, catalyst need not any special packing, and in the beds of the conversion zone of directly packing into, the same as fixed bed reactors, catalyst can directly be packed in the reactor bed by the loading port above the bed, the unload outlet of used catalyst below bed directly emitted, and the filling operation of catalyst is greatly simplified.Because without any packing, so reactant must not diffuse through packaging bag, and directly contacts with catalyst, to reacting very favourable.Like this, one can reduce investment outlay: two can simplify the operation, time saving and energy saving.
The present invention describes in detail:
Catalytic distillation apparatus structure of the present invention as shown in Figure 1.Whole device divides three sections, and epimere is rectifying section＜2 〉, hypomere is stripping section＜4 〉, the middle part is conversion zone＜3 〉.Conversion zone is divided into several beds, establishes separation tray＜10 between two beds 〉.The loadings of catalyst in the tower tray number of rectifying section and stripping section, bed number and each beds is according to determining to reaction conversion ratio and to the requirement of product purity and output.Liquid phase material flows downward to last tower tray of rectifying section by cat head, through downspout＜5〉and liquid seal trough＜6 inflow catalyst bed top＜7, flow downward by gravity then and pass beds＜8 〉, support card＜9 by catalyst bottom〉on metal or nonmetal (can establish stainless steel wire as required) hurdle net flow out, enter the plate below it.When liquid material passes beds, react and emit reaction heat.Be reflected under the bubble point temperature and carry out, reaction heat makes the partial material vaporization, and is constant with the maintenance reaction temperature, and play fractionation, and product is separated because of boiling point is different with reactant, thereby destroy the equilibrium relation of reaction, improves conversion ratio.Absorption reaction heat in beds and the vapour phase part of vaporization, its amount is relevant with conversion ratio, and with liquid phase bubbling and flow out reaction bed downward or upward.By beds＜8〉liquid phase part that flows downward of bottom, flow into next plate＜10〉on, bed steam lifting tube＜11 in the tower tray up and down〉steam that comes up conducts heat, mass transfer, tower tray＜10〉vapour phase part through steam lifting tube＜11 of a last beds enter a last tower tray, the liquid phase part of this tower tray, via downspout＜5〉with liquid seal trough＜6 flow into next bed and proceed reaction, so alternately react continuously and fractional distillation process, end up to reaction, meet the requirements of till the conversion ratio.
After reaction raw materials enters catalytic distillation tower, at conversion zone through after reacting for several times one by one still-process, its low-boiling products is through rectifying section, by overhead line＜12 〉, condenser＜13 〉, enter return tank＜14〉after, its part is via pipeline＜15〉be back to cat head, another part as the low boiling product through pipeline＜16 go out device.The higher boiling product at the bottom of stripping section is by tower through pipeline＜17, enter reboiler＜18 〉, vaporization is after pipeline＜21 return at the bottom of the tower, tower bottom product is through cooler＜19 〉, pipeline＜20 go out device.
As required, can establish at the upper and lower position of each beds the catalyst loading and unloading mouth each one＜22,＜23, be used to load and unload catalyst; Also can between each bed, establish one or several communicating pipe as shown in Figure 2, catalyst is packed into from top bed loading port, use the back to unload outlet and draw off from nethermost one.The top of each beds and bottom preferably all add stainless steel cloth.Can be in the design according to the loading and unloading pattern of tower diameter size, catalyst, the principle that material is evenly distributed, if one or several steam lifting tube＜11 〉, each bed top also can increase a hand hole, in order to the end face of observation, smooth catalyst, as shown in Figure 2.Weir＜24 that exceed the catalyst top should be arranged at the top of steam lifting tube 〉, make the catalyst end face keep certain height of liquid layer, so that distributing uniformly, liquid phase material is downward through bed, it is best that height of weir is generally 30-100mm.
The stripping section of destilling tower＜4〉with rectifying section＜2 tower body, the material that can adopt general designing institute to adopt, middle part conversion zone＜3〉tower body, can optionally adopt stainless steel, steel alloy or carbon steel lining, to prevent corrosion.
Effect of the present invention:
Aforesaid goal of the invention reaches.The present invention can be used for by C
4The synthetic MTBE reaction of isobutene in the fraction and methyl alcohol effect, organic acid and pure esterification reaction, hydration of olefins reaction, the alkylated reaction of chain hydrocarbon or aromatic hydrocarbons, and other reversible balanced reaction.It can improve conversion ratio, simplifies flow process.Can conditioned reaction pressure, changing the bubble point scope of material, and make under the bubble point temperature that is reflected at material and carry out.
Synthesize MTBE as isobutene and methyl alcohol reaction in the C4 fraction:
| Use the present invention | CR8L CO. | |
| Reaction pressure (MPa) reaction temperature (℃) reaction velocity (h -1) conversion ratio (%) | 0.6--1.2 50--90 1--20 90--99.5 | 0.7 70 96.2 |
Claims (7)
1, a kind of catalytic distillation device, i.e. the equipment that the fractionation of catalytic reaction and reactant and product is carried out in same equipment simultaneously is divided into three sections of upper, middle and lower, as shown in Figure 1, top＜2〉be rectifying section, middle part＜3〉be catalyst reaction section, bottom＜4〉be stripping section.The conversion zone that it is characterized in that the middle part comprises several beds＜8 〉, between per two beds tower tray＜10 are arranged 〉, steam lifting tube＜11 〉, weir＜24 〉, catalyst supports card＜9 〉, upper and lower hurdle net, downspout＜5 〉, fluid-tight＜6, or/and catalyst communicating pipe parts such as (as Fig. 2).
2,, it is characterized in that in bulk the shakeouing of catalyst is placed on catalyst support card＜9 by the described catalyst reaction section of claim 1〉on, and between upper and lower hurdle net, do not need conventional method like that catalyst to be divided into many parcels and load.
3, by claim 1,2 described hurdle nets, it is characterized in that the material of hurdle net, can establish stainless steel cloth or glass wool cloth as required with woven wire or nonmetal silk screen.
4,, it is characterized in that steam lifting tube＜11 of catalytic reaction by the described equipment of claim 1〉end face, weir＜24 should be arranged 〉, best height is 30-100mm.
5, by the described tower tray of claim 1＜10 〉, it is characterized in that tower tray can be the tower tray of sieve-plate tower, valve tower or other pattern; Also can be the various packed towers of certain altitude.
6, by the described equipment of claim 1, it is characterized in that the method for catalyst loading and unloading can be by the form of Fig. 1; Also can carry out the charge and discharge operations of catalyst by the form of Fig. 2.
7, by described equipment of claim 1-6 and antigravity system, it is characterized in that such catalytic distillation device, applicable to C
4The synthetic MTBE of isobutene and methyl alcohol reaction in the fraction, the esterification reaction of organic acid and alcohol, the etherification reaction of alcohol, the alkylated reaction of chain hydrocarbon or aromatic hydrocarbons, hydration of olefins reaction, and other reversible balanced reactions.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88109705 CN1022382C (en) | 1988-11-24 | 1988-11-24 | New catalystic distillation equipment |
| US08/513,664 US5523061A (en) | 1988-11-22 | 1995-05-31 | Equipment for catalytic distillation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88109705 CN1022382C (en) | 1988-11-24 | 1988-11-24 | New catalystic distillation equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1042664A true CN1042664A (en) | 1990-06-06 |
| CN1022382C CN1022382C (en) | 1993-10-13 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 88109705 Expired - Lifetime CN1022382C (en) | 1988-11-22 | 1988-11-24 | New catalystic distillation equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1022382C (en) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1108844C (en) * | 2000-03-22 | 2003-05-21 | 王玲 | Fractionating reaction column plate type catalytic distillating equipment |
| CN100404096C (en) * | 2006-08-15 | 2008-07-23 | 中国石油天然气股份有限公司 | Reaction rectifying tower for producing dimethyl carbonate by using urea alcoholysis method |
| CN102060645A (en) * | 2009-11-17 | 2011-05-18 | 中国石油化工集团公司 | Process for preparing olefins by methanol dehydration |
| CN102690185A (en) * | 2011-03-25 | 2012-09-26 | 苏舍化学技术有限公司 | Reactive distillation process and plant for obtaining acetic acid and alcohol from the hydrolysis of methyl acetate |
| CN102060644B (en) * | 2009-11-17 | 2013-07-10 | 中国石油化工集团公司 | Method for preparing olefin by dehydration of methanol |
| CN103421532A (en) * | 2012-05-15 | 2013-12-04 | 中国石油化工股份有限公司 | Solid acid alkylation reaction method |
| CN103706309A (en) * | 2013-12-17 | 2014-04-09 | 西南化工研究设计院有限公司 | Reaction rectification reactor |
| CN104841149A (en) * | 2015-06-05 | 2015-08-19 | 中建安装工程有限公司 | Device and method for preparing high-purity methyl tertiary butyl ether by using partitioning plate catalytic rectifying tower |
| CN105561615A (en) * | 2014-10-09 | 2016-05-11 | 中国石油化工股份有限公司 | Catalysis rectification apparatus and applications thereof |
| CN107519657A (en) * | 2017-09-26 | 2017-12-29 | 丹东明珠特种树脂有限公司 | A kind of catalytic distillation module applied to etherification reaction |
| CN110172013A (en) * | 2019-06-24 | 2019-08-27 | 中国石油化工股份有限公司 | A kind of technique based on catalytic distillation solvent method synthesis tert-pentyl alcohol |
| CN112934137A (en) * | 2021-01-28 | 2021-06-11 | 常州飞达新材料科技有限公司 | Multi-layer packed bed micro-reactor for benzocaine and reaction method |
-
1988
- 1988-11-24 CN CN 88109705 patent/CN1022382C/en not_active Expired - Lifetime
Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1108844C (en) * | 2000-03-22 | 2003-05-21 | 王玲 | Fractionating reaction column plate type catalytic distillating equipment |
| CN100404096C (en) * | 2006-08-15 | 2008-07-23 | 中国石油天然气股份有限公司 | Reaction rectifying tower for producing dimethyl carbonate by using urea alcoholysis method |
| CN102060645A (en) * | 2009-11-17 | 2011-05-18 | 中国石油化工集团公司 | Process for preparing olefins by methanol dehydration |
| CN102060644B (en) * | 2009-11-17 | 2013-07-10 | 中国石油化工集团公司 | Method for preparing olefin by dehydration of methanol |
| CN102060645B (en) * | 2009-11-17 | 2013-07-24 | 中国石油化工集团公司 | Process for preparing olefins by methanol dehydration |
| CN102690185A (en) * | 2011-03-25 | 2012-09-26 | 苏舍化学技术有限公司 | Reactive distillation process and plant for obtaining acetic acid and alcohol from the hydrolysis of methyl acetate |
| CN102690185B (en) * | 2011-03-25 | 2015-11-18 | 苏舍化学技术有限公司 | For being hydrolyzed methyl acetate to obtain the reactive distillation method and apparatus of acetic acid and alcohol |
| US9045412B2 (en) | 2011-03-25 | 2015-06-02 | Sulzer Chemtech Ag | Reactive distillation process and plant for obtaining acetic acid and alcohol from the hydrolysis of methyl acetate |
| CN103421532A (en) * | 2012-05-15 | 2013-12-04 | 中国石油化工股份有限公司 | Solid acid alkylation reaction method |
| CN103421532B (en) * | 2012-05-15 | 2015-07-29 | 中国石油化工股份有限公司 | A kind of solid acid alkylating reaction method |
| CN103706309B (en) * | 2013-12-17 | 2015-08-12 | 西南化工研究设计院有限公司 | A kind of reactive distillation reactor |
| CN103706309A (en) * | 2013-12-17 | 2014-04-09 | 西南化工研究设计院有限公司 | Reaction rectification reactor |
| CN105561615A (en) * | 2014-10-09 | 2016-05-11 | 中国石油化工股份有限公司 | Catalysis rectification apparatus and applications thereof |
| CN105561615B (en) * | 2014-10-09 | 2018-05-04 | 中国石油化工股份有限公司 | catalytic distillation device and application |
| CN104841149A (en) * | 2015-06-05 | 2015-08-19 | 中建安装工程有限公司 | Device and method for preparing high-purity methyl tertiary butyl ether by using partitioning plate catalytic rectifying tower |
| CN107519657A (en) * | 2017-09-26 | 2017-12-29 | 丹东明珠特种树脂有限公司 | A kind of catalytic distillation module applied to etherification reaction |
| CN107519657B (en) * | 2017-09-26 | 2022-11-29 | 丹东明珠特种树脂有限公司 | Catalytic rectification module applied to etherification reaction |
| CN110172013A (en) * | 2019-06-24 | 2019-08-27 | 中国石油化工股份有限公司 | A kind of technique based on catalytic distillation solvent method synthesis tert-pentyl alcohol |
| CN110172013B (en) * | 2019-06-24 | 2023-06-16 | 中国石油化工股份有限公司 | Process for synthesizing tertiary amyl alcohol based on catalytic distillation solvent method |
| CN112934137A (en) * | 2021-01-28 | 2021-06-11 | 常州飞达新材料科技有限公司 | Multi-layer packed bed micro-reactor for benzocaine and reaction method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1022382C (en) | 1993-10-13 |
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| C15 | Extension of patent right duration from 15 to 20 years for appl. with date before 31.12.1992 and still valid on 11.12.2001 (patent law change 1993) | ||
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Owner name: CHINA PETROLEUM & CHEMICAL CORPORATION Free format text: FORMER OWNER: INST. OF QILU PETRO-CHEMICAL INDUSTRY CO. Effective date: 20070727 |
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| C41 | Transfer of patent application or patent right or utility model | ||
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Effective date of registration: 20070727 Address after: 100029, No. 6, Xin Xin Street East, Beijing, Chaoyang District Patentee after: Sinopec Corp. Address before: 129 mailbox, Zibo City, Shandong Province Patentee before: Inst. of Qilu Petro-Chemical Co. |
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| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |