CN204637623U - Acetic acid rectifying and dewatering Tower System - Google Patents
Acetic acid rectifying and dewatering Tower System Download PDFInfo
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- CN204637623U CN204637623U CN201520221456.0U CN201520221456U CN204637623U CN 204637623 U CN204637623 U CN 204637623U CN 201520221456 U CN201520221456 U CN 201520221456U CN 204637623 U CN204637623 U CN 204637623U
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Abstract
The utility model relates to acetic acid rectifying and dewatering Tower System, comprise dehydrating tower body, dehydrating tower condenser and dehydrating tower return tank, the entrance of described dehydrating tower condenser is communicated by the top of pipeline with dehydrating tower body, the outlet of described dehydrating tower condenser is communicated by the entrance of pipeline with dehydrating tower return tank, described dehydrating tower return tank has two outlets, one of them outlet is communicated with acetic acid reaction still by drawing liquid pump pipeline, another outlet is communicated with dehydrating tower body by drawing liquid pump pipeline, it is characterized in that: in described dehydrating tower return tank, be provided with organic membrane filter cylinder, the other end of the described outlet communicated with acetic acid reaction still communicates with cartridge filter inside.The utility model arranges cartridge type organic film in dehydrating tower return tank, allows the penetration by water film of polarity, and other organic matter does not penetrate, and like this water is directly released, and returns acetic acid reaction still as system water supplement with pump.So namely, reduce consumption, turn improve dehydrating tower operational capacity, improve device capbility simultaneously.
Description
Technical field
Of the present utility modelly relate to coal chemical technology, relate to a kind of acetic acid rectifying and dewatering Tower System with membrane separation device particularly.
Background technology
Rectifying is a very important link in petrochemical industry, oil refining production process, its objective is by Component seperation each in mixture out, reaches the purity of regulation.
Rectifying utilizes each component boiling point in mixture different, utilizes heat source mixture, make each material condensation separation at different temperatures, meet the requirements of products of separated purity, meet need of production.Rectifying mode is a lot, and wherein distillation is the typical unit operation of separation of liquid mixtures.It causes gas, liquid two-phase system by heating, utilizes characteristic that in system, each component volatilization degree is different to realize the object of separation.Distillation can be divided into simple distillation by distillation mode, equlibrium distillation, rectifying and special extract rectification.Below the development of special extract rectification and concrete separate mode.
The general principle of sequence of constant boiling and rectification adds three components in the mixed liquor be separated, and to improve the relative volatility between component, thus they is separated by the method for rectifying.During sequence of constant boiling and rectification, in separated binary liquid mixture, add three components, this component can form minimum azeotrope with one or two components in original solution, thus defines the rectification system of " azeotrope-pure component ".Azeotrope steams from tower top, and pure component is discharged at the bottom of tower, and wherein added three components is called nonvariant boiling reagent or entrainer.
Determine that the key of sequence of constant boiling and rectification feasibility and economy is the selection of nonvariant boiling reagent, azeotropic dosage is the important parameter affecting sequence of constant boiling and rectification Process Design.It is the alcohol-water separation process of entrainment reagent that Laroche etc. have studied with benzene, obtains the Changing Pattern changing light component relative volatility when carrying under one's arms dosage.
Relation between entrainment agents dosage and product quality is also attached most importance to by the research direction from now on for sequence of constant boiling and rectification, reaches efficient high yield.Traditional constant boiling rectification method has formed the very high absolute alcohol production technology of scale, mechanization degree, and output is large, quality is good, administration measure, technology maturation, and its energy consumption is lower than extractive distillation method, and cost is lower.
Extracting rectifying is identical with sequence of constant boiling and rectification general principle, just comes to distinguish with sequence of constant boiling and rectification according to three components role in distillation process.
Extracting rectifying be enlarge markedly the very little or easy formation azeotropic mixture of relative volatility by adding suitable mass separation agent (MSA) in distillation system component of mixture between relative volatility, make separation be easy to carry out, thus obtain a kind of special extract rectification technology of product.Although extracting rectifying adds the relative volatility between separated component on the one hand, separation is carried out, the disadvantage brought on the other hand is that ratio of solvent is large, thus causes production capacity raising to be met difficulty, and process energy consumption is large.In order to solve this drawback, be the selection from " stream " the i.e. tower plate structure of extracting rectifying flow arrangement, extractive distillation column and " field " i.e. release agent or solvent to the study general of extracting rectifying process, to separation of extractive distillation process development and perfect.
Current study hotspot how to select suitable extractant, and the conventional method of selective solvent is the approximate range first adopting character leash law to delimit solvent needed for separating mixture system.For a separated system, often can obtain multiple applicable solvent by this method, then appliance computer optimization method seeks the direction that optimum solvent has become research.When extraction rectification technique route and solvent inconvenience are changed, adopting the column plate inner member of new high-efficiency, is the available strategy improving extractive distillation column production capacity.
Nineteen twenty-one Bacchaus first proposed the concept of reactive distillation, and reactive distillation chemical reaction is separated a kind of coupling process being combined in same equipment and carrying out.In 20 century 70 mid-terms, first Eastman Kodak company achieves the homogeneous reaction distillation process industrialization that esterification and extracting rectifying combine, and the later stage seventies expands to heterogeneous system.Because the world constantly increases MTBE demand, thus this technology is made to receive extensive concern.
With the process of chemical reaction in catalytic distillation process, owing to being separated and the strong reciprocation of reaction, make the theoretical modeling of this process and engineering design become numerous and diverse, the influence factor of process is a lot, to its research than traditional reaction and rectifying much more difficult.Although catalytic rectification process proposes very early, up to the present, complete theoretical system is not set up yet.
Extracting rectification technique from hydrogenation coal tar, reclaims high-purity benzene develop.Because arene content in coal tar is very high, liquid-liquid extraction technique is just no longer applicable, and polar solvent is applicable to this kind of situation.In extracting rectification technology, the factor of decision is the ability that solvent changes hydrocarbon vapours pressure in mixture, and this effect is caused by the polar structure of solvent molecule, and causes the vapour pressure of all hydro carbons in solution to reduce, but degree is different.The principle of extracting rectification is exactly first by ends removal close for boiling point, then mixes with polar solvent, improves boiling-point difference, increases the volatility of non-aromatics, and removes azeotropic mixture.
Traditional rectifying device energy consumption is large, and thermodynamic efficiency is very low.To this, there has been proposed many conservation measures.A large amount of theory analysises, experimental study and commercial Application show, the energy-saving effect of heat pump distillation is very remarkable.Heat pump distillation is that rectifying column tower top steam pressurized is heated up, and makes it be used as the thermal source of tower bottom reboiler, reclaims the condensation latent heat of overhead vapours.Different according to the outside energy that heat pump consumes, heat pump distillation can be divided into steam compression type and steam-sprayed two types.
The dehydrating tower rectification process that existing acetic acid plant adopts is simple separated mainly, and adopt float valve tray to carry out being separated of acetic acid and water, steam energy consumption is higher, and concrete operations technological process is as follows.
Lightness-removing column rectifying section has a special side line plate, it is by the whole extraction of thick acetic acid of moisture and a small amount of iodomethane, by thick sour collecting tank through dehydrating tower feed pump, small part is returned lightness-removing column and is refluxed as tower hypomere, major part enters dehydrating tower, thick acetic acid water content is about 10%, and the water in thick acetic acid is undertaken adding thermal release by steam by float valve tray.In order to avoid the gathering of hydrogen iodide in dehydrating tower, attract second charging of one methyl alcohol as dehydrating tower by low-pressure absorption tower methanol pump, introduce from dehydrating tower bottom, itself and hydrogen iodide are reacted and generates iodomethane and water.Dehydrating tower ejects the gas phase come and enters dehydrating tower condenser, condensing cooling is to 62 DEG C, condensate liquid through dehydrating tower backflash by dehydrating tower reflux pump, reflux back a part of phegma the tower top of dehydrating tower, and a part delivers to acetic synthesis operation reactor and transformation pot by thin acid pump together with the light phase Produced Liquid of lightness-removing column quantizer.
Dehydrating tower kettle liquid is the dry acetic acid that water content is less than 750ppm, sends into finishing column through finishing column feed pump.
Dehydration return tank is entered from the dehydrating tower condenser thick acetic acid that out water content is higher, because an acetic acid part for dehydrating tower return tank water content about 30% out is back to the normal operating that dehydration rectifying is carried out on dehydrating tower top, a part returns synthesis reaction vessel by thin acid pump.There are following two problems in above distillation technology: first is that energy consumption is high, and water content height steam consumption is high in various degree; Second is: the internal structure of equipment needs to be optimized further, is beneficial to overall raising production Technology and running efficiency.
Summary of the invention
The utility model is the further improvement at acetic acid rectifying and dewatering Tower System.Due to traditional acetic acid rectifying employing is tower disc type rectifying, needs a large amount of steam to heat in production process, and producing steam needs coal combustion, can have large quantity of exhaust gas and discharge of wastewater, have greater environmental impacts at steam in production process.Overhead gas needs cooling for reflux simultaneously, and recirculated water needs cooling and circulation, and kinetic energy consumes high.The present invention adopts organic film penetration theory and extracting rectification mode to combine, and improves its device systems.
Acetic acid rectifying and dewatering Tower System, comprise dehydrating tower body, dehydrating tower condenser and dehydrating tower return tank, the entrance of described dehydrating tower condenser is communicated by the top of pipeline with dehydrating tower body, the outlet of described dehydrating tower condenser is communicated by the entrance of pipeline with dehydrating tower return tank, described dehydrating tower return tank has two outlets, one of them outlet is communicated with acetic acid reaction still by drawing liquid pump pipeline, another outlet is communicated with dehydrating tower body by drawing liquid pump pipeline, it is characterized in that: in described dehydrating tower return tank, be provided with organic membrane filter cylinder, the other end of the described outlet communicated with acetic acid reaction still communicates with cartridge filter inside.
Described cartridge filter is tubular, is fixed on the port of export of dehydrating tower return tank.
The sidewall of described cartridge filter is hard material, and two bottom surfaces are organic film, and the outlet communicated with acetic acid reaction still is fixed on sidewall.
The utility model arranges cartridge type organic film in dehydrating tower return tank, allows the penetration by water film of polarity, and other organic matter does not penetrate, and like this water is directly released, and returns acetic acid reaction still as system water supplement with pump.So namely, reduce consumption, turn improve dehydrating tower operational capacity, improve device capbility simultaneously.
The utility model compared with prior art has following beneficial effect: 1, reduce water at dehydrating tower Inner eycle, reduce steam consumption; 2, in advance water Returning reacting system, because reaction system water content in acetic acid carbonylation synthesis technology requires about 12%, otherwise catalyst fluctuation of service, former technique acetic synthesis system needs supplementary fresh water, timely like this water is returned acetic synthesis reactor, ensure that the stability of acetic synthesis system.3, improve the disposal ability of dehydrating tower, improve device capbility.4, product quality is ensured.
Accompanying drawing explanation
Fig. 1 is acetic acid rectifying and dewatering Tower System structural representation.
In Fig. 1, each several part Reference numeral is respectively: 1: dehydrating tower body, 2: dehydrating tower condenser, 3: cartridge filter, 4: organic film, 5: dehydrating tower return tank, 6: reflux pump, 7: drawing liquid pump, 8: drawing liquid pump outlet, 9: acetic acid reaction still.
Detailed description of the invention
As shown in Figure 1, the present invention proposes a kind of acetic acid rectifying and dewatering Tower System, comprise dehydrating tower body 1, dehydrating tower condenser 2 and dehydrating tower return tank 5, the entrance of described dehydrating tower condenser 2 is communicated by the top of pipeline with dehydrating tower body 1, the outlet of described dehydrating tower condenser 2 is communicated by the entrance of pipeline with dehydrating tower return tank 5, organic membrane filter cylinder 3 is provided with in described dehydrating tower return tank 5, described dehydrating tower return tank 5 has two outlets, one of them exit end communicates with cartridge filter 3 inside, the other end carries out the extracting of water by drawing liquid pump 7, then send into acetic acid reaction still 9 by drawing liquid pump outlet 8 to communicate, another outlet is communicated with dehydrating tower body 1 by reflux pump 6 pipeline.
Described cartridge filter 3 is tubular, and two bottom surfaces are organic film 4, allows the penetration by water film of polarity, and other organic matter does not penetrate.
Concrete operation flow process is as follows:
Dehydration return tank is entered from the dehydrating tower condenser thick acetic acid that out water content is higher, former technique remains unchanged, an acetic acid part for dehydrating tower return tank water content about 30% out is back to the normal operating that dehydration rectifying is carried out on dehydrating tower top, and a part returns synthesis reaction vessel by thin acid pump.In view of this process condition, in dehydrating tower return tank, increase cartridge filter, organic film is wrapped in filter cylinder outside, allows the penetration by water film of polarity enter in filter cylinder, directly the water of distillation system dehydrating tower is returned acetic acid reaction still in time by drawing liquid pump.Production system can be adjusted in time according to dehydrating tower ruuning situation and reaction system water content situation in actual mechanical process, guarantee front and back system stability.
The thick acid major part of former acetic acid distillation system is in the rectifying of dehydrating tower Inner eycle, and be separated this part water, dehydrating tower thermic load is large, and steam consumption is high.And the water capacity of synthesis system easily after move to distillation system, easily there is fluctuation in synthesis reaction system, after increasing organic membrane filter cylinder can in advance be perforated through film containing more than 90% water turn back to reaction system, ensure that system stable operation.Reduce the steam consumption of distillation system simultaneously.
It should be noted that above-described embodiment is only for the utility model example is clearly described, and be not the restriction to embodiment of the present utility model.For those of ordinary skill in the field, other multi-form change or change can also be made on the basis of the above description.All within spirit of the present utility model and principle, any amendment made, equivalent replacement, improvement etc. are all included among protection domain of the present utility model.
Claims (3)
1. acetic acid rectifying and dewatering Tower System, comprise dehydrating tower body, dehydrating tower condenser and dehydrating tower return tank, the entrance of described dehydrating tower condenser is communicated by the top of pipeline with dehydrating tower body, the outlet of described dehydrating tower condenser is communicated by the entrance of pipeline with dehydrating tower return tank, described dehydrating tower return tank has two outlets, one of them outlet is communicated with acetic acid reaction still by drawing liquid pump pipeline, another outlet is communicated with dehydrating tower body by drawing liquid pump pipeline, it is characterized in that: in described dehydrating tower return tank, be provided with organic membrane filter cylinder, the other end of the described outlet communicated with acetic acid reaction still communicates with cartridge filter inside.
2. acetic acid rectifying and dewatering Tower System according to claim 1, is characterized in that: described cartridge filter is tubular, is fixed on the port of export of dehydrating tower return tank.
3. acetic acid rectifying and dewatering Tower System according to claim 2, is characterized in that: the sidewall of described cartridge filter is hard material, and two bottom surfaces are organic film, and the outlet communicated with acetic acid reaction still is fixed on sidewall.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201520221456.0U CN204637623U (en) | 2015-04-13 | 2015-04-13 | Acetic acid rectifying and dewatering Tower System |
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| CN201520221456.0U CN204637623U (en) | 2015-04-13 | 2015-04-13 | Acetic acid rectifying and dewatering Tower System |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021047393A1 (en) * | 2019-09-10 | 2021-03-18 | 上海浦景化工技术股份有限公司 | Rectification device and rectification method for oxo synthesis of acetic acid |
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2015
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2021047393A1 (en) * | 2019-09-10 | 2021-03-18 | 上海浦景化工技术股份有限公司 | Rectification device and rectification method for oxo synthesis of acetic acid |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 463800 south side of Xingye Road East, Shangcai, Zhumadian, Henan Patentee after: HENAN SHUNDA NEW ENERGY TECHNOLOGY Co.,Ltd. Address before: 463800 south side of Xingye Road East, Shangcai, Zhumadian, Henan Patentee before: Henan Shunda new energy Co.,Ltd. |
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| CP01 | Change in the name or title of a patent holder | ||
| CP03 | Change of name, title or address |
Address after: 463800 south side of Xingye Road East, Shangcai, Zhumadian, Henan Patentee after: Henan Shunda new energy Co.,Ltd. Address before: 463000 439 Zhonghua Road, Yicheng District, Zhumadian, Henan Patentee before: HENAN SHUNDA CHEMICAL SCIENCE & TECHNOLOGY CO.,LTD. |
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| CP03 | Change of name, title or address | ||
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of utility model: Acetic acid rectification and dehydration tower system Effective date of registration: 20191012 Granted publication date: 20150916 Pledgee: Zhumadian Rural Commercial Bank Co.,Ltd. Pledgor: HENAN SHUNDA NEW ENERGY TECHNOLOGY Co.,Ltd. Registration number: Y2019980000246 |
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| PE01 | Entry into force of the registration of the contract for pledge of patent right | ||
| PC01 | Cancellation of the registration of the contract for pledge of patent right |
Date of cancellation: 20200522 Granted publication date: 20150916 Pledgee: Zhumadian Rural Commercial Bank Co.,Ltd. Pledgor: HENAN SHUNDA NEW ENERGY TECHNOLOGY Co.,Ltd. Registration number: Y2019980000246 |
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| PC01 | Cancellation of the registration of the contract for pledge of patent right |