CN100575326C - Improved acetic acid purifying device - Google Patents
Improved acetic acid purifying device Download PDFInfo
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- CN100575326C CN100575326C CN200610029928A CN200610029928A CN100575326C CN 100575326 C CN100575326 C CN 100575326C CN 200610029928 A CN200610029928 A CN 200610029928A CN 200610029928 A CN200610029928 A CN 200610029928A CN 100575326 C CN100575326 C CN 100575326C
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Abstract
A kind of improved acetic acid purifying device, comprise lightness-removing column, dehydration tower, weight-removing column and the waste acid column of refining system and the decanting vessel of air-washing system and the setting of lightness-removing column top, it is characterized in that, before lightness-removing column, increase by a multipurpose tower, produce the first acetic acid contain acetic acid about 50% from flash drum by flash distillation and be connected to first acetic acid import on many kinetic energy tower by pipeline, cat head at multipurpose tower connects an absorption liquid pipeline and a gaseous phase materials pipeline, absorption liquid adds multipurpose tower from the absorption liquid pipeline, and described gaseous phase materials pipeline is connected to lightness-removing column; At tower bottom one heavy phase material pipe is set and is connected to reactive system.The present invention can adapt to the catalyzer of the synthetic acetic acid technology of low pressure methanol carbonylation and form any one variation range, especially high methyl iodide concentration, high ritalin concentration, low water concentration catalyst system.Acetic acid synthesized reaction yield improves, and the less side products of reaction is improved equipment simultaneously, cuts down the consumption of energy.
Description
Technical field
The present invention relates to a kind of purifying plant of acetic acid synthesized by low pressure methanol carbonylation, particularly catalyzer is formed improved acetic acid purifying device to high Primary Catalysts concentration, high methyl iodide concentration, high ritalin concentration, low water concentration trend development in the synthetic acetic acid technology of low pressure methanol carbonylation.
Technical background
Acetic acid is important chemical intermediate and chemical reaction solvent.With carbon monoxide and methyl alcohol is raw material, produces acetic acid with oxo synthesis.Developed the production technique of acetic acid synthesized by low pressure methanol carbonylation since U.S. Monsanto Company after, the acetic acid synthesized by low pressure methanol carbonylation technology becomes the main method of producing acetic acid in the world at present.
At present, the production process equipment of acetic acid synthesized by low pressure methanol carbonylation is seen Fig. 1, mainly comprises reactor 1, four towers of refining system (lightness-removing column 2, dehydration tower 3, weight-removing column 4, waste acid column 5), and scrubbing tower 6, distillation tower condensation liquid bath 7.Add reactor 1 bottom with carbon monoxide, catalyzer etc. after the methyl alcohol preheating, under certain temperature and pressure, react, reaction solution is drawn in the top of reactor 1 side line in the reaction back, decompression makes reaction product separate with the mother liquor that contains catalyzer, latter's Returning reactor 1 (reactor 1 expellant gas contains carbon monoxide, methyl iodide, hydrogen, methane sends into scrubbing tower 6).The reaction mixture that contains thick acetic acid, lighting end enters first tower-lightness-removing column 2 of refining system with gas phase, deviates from lighting end, and the gas of cat head enters scrubbing tower through 7 of distillation tower condensation liquid baths.The still liquid of lightness-removing column 2 is moisture thick acetic acid, is sent to dehydration tower 3, and the dry crude acetic acid of dehydration tower 3 bottoms is admitted to weight-removing column 4 again.Draw finished acid from weight-removing column 4 top side lines; It is waste acid column 5 that acetic acid in weight-removing column 4 bottom fraction is sent to the 4th tower at last, to recycle.Consist of CO 40～80% after three towers and reactor 1 expellant gas gather, all the other 20～60% are H
2, CO
2, N
2, O
2And acetic acid, the methyl iodide of trace,
Composition change along with catalyzer: water content in catalyzer reduces on the one hand; Ritalin and methyl iodide content in catalyzer increases on the other hand.Moreover the inorganic iodine salt stabilizing agent suppresses evaporation of water in flash vaporization process, promotes the evaporation of acetic acid, ritalin and methyl iodide.The effect of two aspects makes that the content of ritalin and methyl iodide obviously increases in the lightness-removing column 2 into, ritalin content is at 5～6% (wt), methyl iodide content is at 35～50% (wt), make that ritalin and methyl iodide concentration improve in the inner gas phase of this tower, ritalin and methyl iodide also obviously increase in the fluid of trim the top of column, cause the head product acetic acid of extracting out from lightness-removing column 2, though moisture reduction but the amount of ritalin and methyl iodide obviously increase, caused containing ritalin in the discharging of dehydration tower 3 and the feed stream and methyl iodide increases, especially ritalin and methyl iodide content increase in the trim the top of column thing, caused this tower product to be polluted by ritalin and methyl iodide, so under the prerequisite that catalyzer changes, the technology of purification acetic acid also needs new improvement.
Prepare the method for acetic acid this by methanol carbonyl, disclose by reducing the amount that the water yield in the carbonylation reactor can reduce by product (carbonic acid gas and propionic acid).In addition, suggestion is simplified the purification process that obtains acetate products by the water yield that reduces in the reactor.Yet, when the water yield in the carbonylation reactor reduces, in the trace impurity of by-product, containing some components, the amount of these components increases along with the increase of acetate yield, and these components have reduced the quality of acetate products.
The purification schemes of BP, contest road Dichlorodiphenyl Acetate has been done research, has carried out the improvement of purifying technique, and BP has explained the change that the technology that adopts single rectification zone is come catalyzer in the adaptive response liquid in Chinese patent application 93108283; And the contest road is controlled the stratified temperature of decanting vessel and add water transformation acetic acid purification schemes in material at first distillation tower in Chinese patent application 96190401.
The angle of the carbon dioxide by-product amount that forms from control propionic acid by-product amount and shift reaction, the concentration of contained water is preferably lower in this carbonyl reaction liquid.Yet, in reducing this carbonyl reaction liquid, during the concentration of contained water, reduced liquid separability in this lightness-removing column top decanting vessel, and just stopped separation within a short period of time.Consequently, owing to reduced the concentration of its water, when the concentration of water contained in this carbonyl reaction liquid is higher, sneak into easily from this lightness-removing column bottom or near the isolated thick acetic acid of its bottom side cut by being back to the impurity that takes to wherein at the lightness-removing column top.
Be provided with decanting vessel 8 in the Chinese patent application 96190401 behind the cat head vapor condensation of lightness-removing column, so that isolate gas phase at decanting vessel 8 behind the cat head vapor condensation, isolate two liquid phases then, one mainly contains methyl-iodide mutually, and another mainly contains water mutually.The methyl-iodide that wherein is dissolved with many impurity is extracted out as the lower boiling circulating fluid, but after separation stopped, the liquid that a part contains these impurity was added in the lightness-removing column as phegma, so these impurity are blended in the acetic acid easily.
In addition, present purifying technique, in taking off light phase step, I in the solution
-Concentration ratio is higher, and it is abundant inadequately to change into methyl iodide, can pollute the logistics that enters dehydration tower, to follow-up dehydrating step with take off the heavy phase step and pollute, has influence on the effect of purification.
Also have, present purifying technique is that drop temperature is 140 ℃ from the side line discharging of weight-removing column, and acetic acid stores that to need temperature be below 38 ℃, and the energy consumption of side line extraction product cooling needs is very high like this.And for large-size chemical manufacturing enterprise, energy-conservation is very important.
Summary of the invention
One of technical problem to be solved by this invention is to provide a kind of purifying plant that is fit to above-mentioned method of purification, the catalyzer that can adapt to the synthetic acetic acid technology of low pressure methanol carbonylation is formed any one variation range, especially high methyl iodide concentration, high ritalin concentration, low water concentration catalyst system.It enters the thick acetic acid foreign matter content of lightness-removing column head product by reduction, and the purifying energy consumption is controlled at lower degree, improves the productive rate of acetic acid.
A kind of improved acetic acid synthesized by low pressure methanol carbonylation purifying plant of the present invention, the lightness-removing column that comprises refining system, dehydration tower, weight-removing column and waste acid column and air-washing system and the decanting vessel that the setting of lightness-removing column top is set, it is characterized in that, before lightness-removing column, increase by a multipurpose tower, produce the first acetic acid contain acetic acid about 50% from flash drum by flash distillation and be connected to first acetic acid import on many kinetic energy tower by pipeline, cat head at multipurpose tower connects an absorption liquid pipeline and a gaseous phase materials pipeline, absorption liquid adds multipurpose tower from the absorption liquid pipeline, and described gaseous phase materials pipeline is connected to lightness-removing column; At tower bottom one heavy phase material pipe is set and is connected to reactive system.
Among the present invention, connect a tower bottom reboiler in the multipurpose tower bottom.
Described multipurpose tower is packing tower or tray column.Have 1-5 theoretical stage in this multipurpose tower, preferable is 2-3 theoretical stage.
Among the present invention, described gaseous phase materials pipeline is connected to the middle and upper part of lightness-removing column, and connects a methanol pipeline of carrying methyl alcohol in the bottom of lightness-removing column.
Described lightness-removing column is packing tower or tray column.Have 15-30 theoretical stage in this lightness-removing column, preferable is 20-30 theoretical stage.
Described lightness-removing column contains the profit reduction and reserving section and the rectifying section of rectifying tower, wherein the gaseous phase materials conduit entrance is above is rectifying section, below is the profit reduction and reserving section, and it is 5-15 that rectifying section has theoretical stage, it is 10-25 that the profit reduction and reserving section has theoretical stage, and the import of described methanol pipeline is positioned at the mid-way of profit reduction and reserving section.Preferable, it is 5-10 that described rectifying section has theoretical stage, it is 10-15 that the profit reduction and reserving section has theoretical stage.
Connect a tower bottom reboiler in described lightness-removing column bottom.
The wet acetic acid transport pipe of described lightness-removing column bottom is connected to the middle part of described dehydration tower.
The overhead condenser that passes through at described lightness-removing column top connects decanting vessel.
One water inlet pipe is set, to keep adding water on described decanting vessel.The reflux pipe material of described decanting vessel connects the refluxing opening and the reactive system of lightness-removing column.
Described dehydration tower is packing tower or tray column.Have 25-35 theoretical stage in this dehydration tower.
The cat head of described dehydration tower is provided with by the condenser of pipe connection and phlegma storage tank, and the phlegma pipeline of described phlegma storage tank connects the refluxing opening and the reactive system of dehydration tower.
Methyl alcohol import on the described dehydration tower is arranged in the mid-way of dehydration tower profit reduction and reserving section.Described methyl alcohol import allows to change up and down a theoretical stage.
Connect a tower bottom reboiler in described dehydration tower bottom.
The dried acetic acid transport pipe of described dehydration tower bottom connects described weight-removing column.
Described weight-removing column has 30-45 theoretical stage, and preferable is 35-45 theoretical stage.
The cat head of described weight-removing column is provided with by the condenser of pipe connection and phlegma storage tank, and the phlegma pipeline of described phlegma storage tank connects the refluxing opening and and the product extraction mouth of dehydration tower.
Connect a tower bottom reboiler in described weight-removing column bottom.
Improved acetic acid synthesized by low pressure methanol carbonylation purifying plant of the present invention, the catalyzer that can adapt to the synthetic acetic acid technology of low pressure methanol carbonylation is formed any one variation range, especially high methyl iodide concentration, high ritalin concentration, low water concentration catalyst system.By technical process correspondingly, acetic acid synthesized reaction yield is improved, the less side products of reaction is improved equipment simultaneously, cuts down the consumption of energy.
Description of drawings
Further specify the present invention below in conjunction with the drawings and specific embodiments.
Fig. 1 be Meng Shan all the low pressure methanol carbonylation produce the device synoptic diagram of acetic acid.Among the figure: 1 is reactive system; 2 is lightness-removing column; 3 is dehydration tower; 4 is weight-removing column; 5 is waste acid column; 6 is air-washing system; 7 is distillation tower condensation liquid bath.
Fig. 2 is the purifying plant synoptic diagram that improved low pressure methanol carbonylation is produced acetic acid.Among the figure: the 2-lightness-removing column; The 3-dehydration tower; The 4-weight-removing column; The 5-waste acid column; The 6-air-washing system; 7,15-distillation tower condensation liquid bath; The 8-multipurpose tower; 9,12,13,17,18-tower bottom reboiler; 10,14,16 overhead condensers; The 11-decanting vessel.
Embodiment
For technique means, creation characteristic that the present invention is realized, reach purpose and effect is easy to understand, below in conjunction with embodiment, further set forth the present invention.Below in conjunction with the concrete technological process of production, describe the function of apparatus of the present invention in detail.
Referring to Fig. 2, a kind of improved acetic acid synthesized by low pressure methanol carbonylation purifying plant comprises multipurpose tower 8, lightness-removing column 2, dehydration tower 3, weight-removing column 4, waste acid column 5, air-washing system 6, decanting vessel 11, distillation tower phlegma storage tank 7,15, tower bottom reboiler 9,12,13,17,18, overhead condenser 10,14,16.
Produce the first acetic acid 19 contain acetic acid about 50% from flash drum by flash distillation and be connected to first acetic acid import on many kinetic energy tower 8 by pipeline, cat head at multipurpose tower 8 connects an absorption liquid pipeline and a gaseous phase materials pipeline, absorption liquid 41 adds multipurpose tower 8 from the absorption liquid pipeline, and gaseous phase materials pipeline 20 is connected to lightness-removing column 2; In multipurpose tower 8 bottoms one heavy phase material pipe 44 is set and is connected to reactive system.And connect a tower bottom reboiler 9 in multipurpose tower 8 bottoms.
Connect a methanol pipeline of carrying methyl alcohol 43 in the bottom of lightness-removing column 2, lightness-removing column 2 tops pass through an overhead condenser 10 and pipeline 22,23 connects decanting vessel 11; The wet acetic acid transport pipe of lightness-removing column 2 bottoms is connected to the middle part of dehydration tower 3.
One water inlet pipe 42 is set, to keep adding water on decanting vessel 11.The reflux pipe material 24 of decanting vessel 11 connects the refluxing opening 26 of lightness-removing column 2 and passes through pipeline 27 ligation systems 45.Heavy phase material pipe 25 connects reactive system 45.Connect a tower bottom reboiler 12 in lightness-removing column 2 bottoms.
The cat head of dehydration tower 3 is provided with condenser 14 and the phlegma storage tank 15 that connects by pipeline 29,30, and the phlegma pipeline 31 of phlegma storage tank 15 connects the refluxing opening 32 of dehydration tower 3 and connects reactive system 45 by pipeline 33.Methyl alcohol import on the dehydration tower 3 is arranged in the mid-way of dehydration tower 3 profit reduction and reserving sections.Connect a tower bottom reboiler 13 in dehydration tower 3 bottoms.The dried acetic acid transport pipe of dehydration tower 3 bottoms connects weight-removing column 4.
The cat head of weight-removing column 4 is provided with condenser 16 and the phlegma storage tank 7 that connects by pipeline 40, and the phlegma pipeline 37 of phlegma storage tank 7 connects the refluxing opening 38 and and the product extraction mouth 36 of dehydration tower 4.Connect a tower bottom reboiler 17 in weight-removing column 3 bottoms and connect waste acid column 5, at the bottom of the tower of waste acid column 5, connect a tower bottom reboiler 18 and a delivery pipe 35 by circulating line 34.
Decanting vessel 11, phlegma storage tank 15,7 are connected with air-washing system 6 by pipeline.
Methyl alcohol and CO generate acetic acid under catalyst action in reactor, produce the first acetic acid 19 that contains acetic acid about 50% by flash distillation at flash drum.According to purification techniques of the present invention, 19 directly do not enter the said lightness-removing column 2 of document, are introduced into a multipurpose tower 8.These multipurpose tower 8 collection absorb and steam stripped function: absorption liquid 41 is from the adding of cat head, by the contact of vapour-liquid on column internals, absorbed some of carrying secretly in the first acetic acid 19 and contained iodine impurity and water, tower bottom reboiler 9 keeps component concentrations and flow in the tower material of heavy phase material pipe 44 outputs by the tower still temperature that keeps boiling state, control to add the quantity of steam of reboiler and control multipurpose tower 8.Multipurpose tower 8 cats head are by gaseous phase materials pipeline 20 output gaseous phase materials.
The absorption liquid 41 of this multipurpose tower 8 is one materials that add, rather than the liquid of this Tower System generation itself.This absorption liquid can be the wet acetic acid 21 of lightness-removing column 2 outlet at bottoms, and the aqueous dilute acetic acid that also can lightness-removing column 2 top decanting vessels 11 be produced also can be the aqueous dilute acetic acid in the dehydration tower 3 condensation liquid baths 15.The flow of this absorption liquid 41 is 1%～10wt% of material 19.
This multipurpose tower 8 can be packing tower and tray column, no matter which kind of form tower, this tower has 1～5 theoretical stage, preferred 2～3 theoretical stages.
From the gaseous phase materials that multipurpose tower 8 comes out, enter the middle and upper part of lightness-removing column 2 by gaseous phase materials pipeline 20.Lightness-removing column 2 is different from people's " C1 to acetyls:catalysis and process " said lightness-removing columns in " Catal.Today " 18 (1993) 325-354 in 1993 such as M.J.Howard.Its improvements are: the import of tower gaseous phase materials of the present invention is in the middle and upper part of tower, rather than the bottom; Lightness-removing column of the present invention contains profit reduction and reserving section and rectifying section, and gaseous phase materials pipeline 20 opening for feeds are above to be rectifying section, is the profit reduction and reserving section below 20 imports of gaseous phase materials pipeline; The function of lightness-removing column of the present invention is to isolate just most ritalin and methyl iodide and most water in the acetic acid 19, makes to contain the methyl iodide of ppb level concentration and the ritalin of ppm level in the wet acetic acid 21, and 3% following water; The present invention adds methyl alcohol in lightness-removing column, the I of feasible trace
-Ion changes into methyl iodide, rather than in " chemical encyclopedia " said in dehydration tower 3, add methyl alcohol.Wherein, the add-on of methyl alcohol is 0.05～0.15% of a product acetic acid amount.
Lightness-removing column 2 can be packing tower and tray column, no matter which kind of form tower, lightness-removing column has 15～30 theoretical stages, preferred 20～25 theoretical stages.Lightness-removing column 2 is divided into rectifying section and profit reduction and reserving sections, and wherein to have theoretical stage be 5～15 to rectifying section, preferred 5～10 theoretical stages, and it is 10～25 that the profit reduction and reserving section has theoretical stage, preferred 10～15 theoretical stages.
Lightness-removing column 2 cats head keep refluxing, and reflux and adopt the low density phase.
Lightness-removing column 2 tops are provided with a decanting vessel 11, and the control internal temperature makes and produce layering in the decanting vessel, be divided into moisture and acetic acid and be main low density mutually and contain methyl iodide and ritalin be the master high-density mutually.There is document (Chinese patent application 96190401) to propose this temperature and is controlled at-20～40 ℃.But experiment finds, the material that overhead condenser 10 of the present invention and pipeline 23 are carried is in decanting vessel 11, solidify when being lower than below-18 ℃ in temperature.The present invention finds that decanting vessel 11 internal temperatures are controlled at 28～36 ℃, and this layered effect has met the needs of purification, and lower temperature will be wasted more energy consumption.
Insert water at decanting vessel 11 by water inlet pipe 42, the total amount that amount of water equals the water yield taken away according to the water yield, product and by product that side reaction in the reactor is used deducts the water yield that raw material is brought into.Improved liquid separability in this lightness-removing column top decanting vessel, reduced impurity and be blended into easily from this lightness-removing column bottom or near the isolated thick acetic acid of its bottom side cut.
Except that keeping tower 2 reflux streams 26, all the other return reactor in the decanting vessel 11.
Methyl alcohol 43 adds the implantation site in lightness-removing column 2, directly influenced the purity of wet acetic acid 21.This methyl alcohol 43 adds the too close tower still in implantation site, and then the ritalin and the unreacted methanol of the generation of methyl alcohol and acetic acid are brought wet acetic acid 21 into, influence product purity.This methyl alcohol 43 adds implantation site too close charging opening, then methyl alcohol and I
-Ion deficiency duration of contact causes I
-Ion changes into methyl iodide and fully pollutes wet acetic acid 21 further polluted products inadequately.The position that this methyl alcohol 43 adds should be the position of promptly leaving 4～8 theoretical stages of tower still in the mid-way of profit reduction and reserving section, and it is the position of 5～6 theoretical stages that the invention process adopts.
Wet acetic acid 21 enters the middle part of dehydration tower 3, and condenser 14 and phlegma storage tank 15 are established in dehydration tower 3 tops.Keep trim the top of column mouth 32 to reflux, the logistics of all the other water-containing acetic acids and impurity etc. is by 33 times reactive systems 45 of pipeline.The cold of control condenser 14 keeps reflux temperature at 30～50 ℃.
The heat by regulating tower bottom reboiler 13 and the flow of backflow, keep in the dried acetic acid 28 water-content less than 600ppm, ritalin content less than 100ppm, methyl iodide content less than 20ppb.
Dehydration tower 3 can be packing tower and tray column, no matter which kind of form tower, this tower has 25～35 theoretical stages, preferred 23～28 theoretical stages.Dehydration tower 3 is divided into rectifying section and profit reduction and reserving sections, and wherein to have theoretical stage be 10～15 to rectifying section (charging is more than 21), preferred 11～13 theoretical stages, and it is 10～25 that profit reduction and reserving sections (charging is more than 21) have theoretical stage, preferred 12～15 theoretical stages.
By " acetic acid and derivative thereof " chapter in " chemical encyclopedia " (the 1st edition the 2nd volume was 713 pages in 1991, Chemical Industry Press), dehydration tower 3 still can add suitable methyl alcohol, and this has been known knowledge, is not that the present invention institute is proprietary.What the present invention emphasized is that this adding is the mid-way of dehydration tower 3 profit reduction and reserving sections, allows to change 1 theoretical stage up and down.This add-on can be 0.05～0.1%wt of acetic acid quantum of output.
The present invention also requires emphasis, and control is the key to weight-removing column 4 technological improvements for the concentration of water, ritalin, methyl iodide in the dried acetic acid 28 of dehydration tower 3 bottoms.
Through purifying, the concentration of water, ritalin, methyl iodide has satisfied the requirement of quality product in the dried acetic acid 28 in dehydration tower 3 bottoms, and what can not reach in the dried acetic acid 28 that quality product requires is propionic acid, this impurity and may not meet target level of product quality I
-Ion removes I in weight-removing column 4 and waste acid column 5
-What ionic removed dependence is to add KOH in the dried acetic acid 28.This " acetic acid and derivative thereof " chapter in " chemical encyclopedia " (the 1st edition the 2nd volume was 719 pages in 1991, Chemical Industry Press) has also had narration, is a known knowledge.
Improvement of the present invention is: by the increase of multipurpose tower 8, the technological improvement of lightness-removing column 2 and the technological improvement and the control requirement of interpolation methyl alcohol and dehydration tower 3, make that into the dried acetic acid 28 of weight-removing column 4 removes propionic acid and I
-Outside the ion, satisfied the standard of acetate products, thus weight-removing column 4 do not need to resemble on the disclosed document described from the side line discharging of tower top, but directly from overhead condensation liquid storage tank 7 extraction products.This improvement can improve weight-removing column 4 device structures and cut down the consumption of energy.
The temperature of overhead condensation liquid storage tank 7 extraction is less than 50 ℃, and is about 140 ℃ from tower side line extraction temperature, and acetic acid stores that to need temperature be below 38 ℃.The energy consumption that the cooling of side line extraction product needs is 8.5 times of overhead condensation liquid storage tank 7 extraction products, produces at large-size chemical, and energy-conservation is very important.
Simultaneously, product is from the side line extraction, and the quantity of reflux of tower needs two portions and forms: there is the great variety of backflow volume up and down in the quantity of reflux that output and tower rectifying need at the extraction mouth, product is from 7 extraction of overhead condensation liquid storage tank, and as long as the backflow of tower is the quantity of reflux that tower rectifying needs.The quantity of reflux that product is adopted tower from overhead condensation liquid storage tank 7 is little, the simplicity of design of tower.
Certainly, for weight-removing column 4, the assurance that needs theoretical stage just has the effect of rectifying to guarantee.Require weight-removing column 4 30～45 theoretical stages to be arranged, preferred 35～40 theoretical stages.
Whole purification system operating pressure is in gauge pressure 0 or pressurization, preferred little pressurization: 100～200kpa.
At the composition that first acetic acid 19 keeps in the tables 1, the flow process of pressing flow process (in " chemical encyclopedia " (the 1st edition the 2nd volume was 713 pages in 1991, Chemical Industry Press) " acetic acid and derivative thereof the ") figure one of document narration experimentizes, and measures the composition of each logistics.
Implementation step: with methyl alcohol and CO in reactor under the effect of carbonylating catalyst, generate acetic acid.The reaction solution that will contain catalyzer and product carries out flash distillation.The tail gas that reaction zone produces washs at air-washing system 6, reclaims catalyzer.The first acetic acid 19 that flash distillation produces is deviate from light constituent through the lightness-removing column 2 shown in " figure one flow process ", extracts wet acetic acid 21 out from lightness-removing column 2 side lines then, and wet acetic acid 21 is deviate from water and other impurity in dehydration tower 3.Exsiccant acetic acid is extracted out from dehydration tower 3 bottoms, advances then in weight-removing column 4 and the waste acid column 5 and deviates from propionic acid.Side line obtains qualified product on the top of weight-removing column 4.
Table 1
Embodiment 2:
At the composition that first acetic acid 19 keeps in the tables 2, technical process of the present invention and implementation step are tested, and absorption liquid is 3.5% of a first acetic acid 19 from the shunting of the wet acetic acid 21 of lightness-removing column 2 outlet at bottoms approximately.Measure the composition of each logistics.
Implementation step: with methyl alcohol and CO in reactor under the effect of carbonylating catalyst, generate acetic acid.The reaction solution that will contain catalyzer and product carries out flash distillation.The tail gas that reaction zone produces washs at air-washing system 6, reclaims catalyzer.The first acetic acid 19 that flash distillation produces enters the bottom of multipurpose tower 8, keep a certain amount of absorption liquid 41 at the top of tower, one tower bottom reboiler 9 is arranged in the bottom of tower, the partially liq vaporization that keeps heating tower's still, control evaporating capacity by the control heat, the liquid stripping of the gas that vaporization produces to producing in the multipurpose tower 8.Multipurpose tower 8 keeps 2-3 piece theoretical stage.The gaseous phase materials of multipurpose tower 8 tops by 20 extraction of gaseous phase materials pipeline advances lightness-removing column 2 and deviates from water, ritalin and methyl iodide, and the tower material of multipurpose tower 8 bottom heavy phase material pipes 44 outputs returns reactive system.By said in the embodiment, the gaseous phase materials of gaseous phase materials pipeline 20 extraction enters from the middle and upper part of lightness-removing column 2, enters a certain amount of methyl alcohol 43 in the bottom of lightness-removing column 2.Lightness-removing column 2 has about 20-25 theoretical stage, and the position of the gaseous phase materials charging of gaseous phase materials pipeline 20 extraction is the 5-10 theoretical stage apart from the topmost separator column, and methyl alcohol 43 is at the about 5-6 of a distance tower still theoretical stage.Lightness-removing column 2 cats head keep refluxing, and reflux and adopt the low density phase.Decanting vessel 11 internal temperatures are controlled at 28-36 ℃.Keep adding water in the decanting vessel 11, the total amount that amount of water equals the water yield taken away according to the water yield, product and by product that side reaction in the reactor is used deducts the water yield that raw material is brought into.Except that keeping 26 logistics of lightness-removing column 2 refluxing openings, all the other return reactive system 45 in the decanting vessel 11.Extract the middle part that wet acetic acid 21 enters dehydration tower 3 out from lightness-removing column 2 bottoms.
The logical amount control that the heat control and lightness-removing column 2 refluxing openings 26 of tower bottom reboiler 12 are refluxed, moisture less than 3%wt in the wet acetic acid 21, ritalin and methyl iodide are less than 1%wt.Condenser 14 and phlegma storage tank 15 are established in dehydration tower 3 tops.Keep dehydration tower 3 trim the top of column mouths 32 to reflux, the logistics of all the other water-containing acetic acids and impurity etc. is by 33 times reactive systems 45 of pipeline.The cold of control condenser 14 keeps refluxing opening 32 reflux temperatures at 30-50 ℃.The flow that heat by regulating tower bottom reboiler 13 and refluxing opening 32 reflux, keep in the dried acetic acid 28 water-content less than 600ppm, ritalin content less than 100ppm, methyl iodide content less than 20ppb.Dehydration tower 3 is a 23-28 theoretical stage rectifying column.Dehydration tower 3 is divided into rectifying section and profit reduction and reserving sections, and wherein to need theoretical stage be about 11-13 to rectifying section (charging is more than 21), and profit reduction and reserving section (charging is below a 21) theoretical stage is about 12-15 theoretical stage.Dried acetic acid 28 after the dehydration advances weight-removing column 4.Pass through product extraction mouth 36 extraction products from overhead condensation liquid storage tank 7.Extract spent acid out at waste acid column 5.Weight-removing column 4 is rectifying columns of 35-40 theoretical stage.Whole purification system operating pressure is in 100～200kpa (gauge pressure).
Table 2
Embodiment 3
At the composition that first acetic acid 19 keeps in the tables 3, be a kind ofly to compare moisture lower flash distillation product with table 1, test by technical process of the present invention, see schema 2, absorption liquid is the 4%wt of first acetic acid 19 from the shunting of the wet acetic acid 21 of lightness-removing column 2 outlet at bottoms approximately.Measure the composition of each logistics.
Table 3
Approaching component that composition in first acetic acid 19 maintenance tables 4 is a kind of and table 3 is tried one's best.Carry out and the implementation step test according to technical process of the present invention, absorption liquid is from the shunting of the pipeline 33 aqueous dilute acetic acid in the dehydration tower 3 condensation liquid baths 15, and flow is 1% of first acetic acid approximately.Measure the composition of each logistics.
Table 4
Embodiment 5
Composition in first acetic acid 19 maintenance tables 5.Carry out and the implementation step test according to technical process of the present invention, absorption liquid is from the shunting of the wet acetic acid 21 of lightness-removing column 2 outlet at bottoms, and flow is the 4wt% of first acetic acid approximately.Measure the composition of each logistics.
Table 5
More than show and described ultimate principle of the present invention, principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; that describes in the foregoing description and the specification sheets just illustrates principle of the present invention; the present invention also has various changes and modifications without departing from the spirit and scope of the present invention, and these changes and improvements all fall in the claimed scope of the invention.The claimed scope of the present invention is defined by appending claims and equivalent thereof.
Claims (24)
1, a kind of improvement acetic acid purifying device, comprise lightness-removing column, dehydration tower, weight-removing column and the waste acid column of refining system and the decanting vessel of air-washing system and the setting of lightness-removing column top, it is characterized in that, before lightness-removing column, increase by a multipurpose tower, produce the first acetic acid contain acetic acid about 50% from flash drum by flash distillation and be connected to first acetic acid import on the multipurpose tower by pipeline, cat head at multipurpose tower connects an absorption liquid pipeline and a gaseous phase materials pipeline, absorption liquid adds multipurpose tower from the absorption liquid pipeline, and described gaseous phase materials pipeline is connected to lightness-removing column; At tower bottom one heavy phase material pipe is set and is connected to reactive system; Described gaseous phase materials pipeline is connected to the middle and upper part of lightness-removing column, and connects a methanol pipeline of carrying methyl alcohol in the bottom of lightness-removing column.
2, device according to claim 1 is characterized in that, connects a tower bottom reboiler in the multipurpose tower bottom.
3, device according to claim 1 is characterized in that, described multipurpose tower is packing tower or tray column.
4, device according to claim 1 is characterized in that, has 1-5 theoretical stage in the described multipurpose tower.
5, device according to claim 1 is characterized in that, has 2-3 theoretical stage in the described multipurpose tower.
6, device according to claim 1 is characterized in that, described lightness-removing column is packing tower or tray column.
7, device according to claim 1 is characterized in that, has 15-30 theoretical stage in the described lightness-removing column.
8, device according to claim 1 is characterized in that, has 20-30 theoretical stage in the described lightness-removing column.
9, device according to claim 1, it is characterized in that, described lightness-removing column contains the profit reduction and reserving section and the rectifying section of rectifying tower, wherein the gaseous phase materials conduit entrance is above is rectifying section, below be the profit reduction and reserving section, it is 5-15 that rectifying section has theoretical stage, and it is 10-25 that the profit reduction and reserving section has theoretical stage, and the import of described methanol pipeline is positioned at the mid-way of profit reduction and reserving section.
10, device according to claim 9 is characterized in that, it is 5-10 that described rectifying section has theoretical stage, and it is 10-15 that the profit reduction and reserving section has theoretical stage.
11, device according to claim 1 is characterized in that, connects a tower bottom reboiler in described lightness-removing column bottom.
12, device according to claim 1 is characterized in that, the wet acetic acid transport pipe of described lightness-removing column bottom is connected to the middle part of described dehydration tower.
13, device according to claim 1 is characterized in that, the overhead condenser that passes through at described lightness-removing column top connects decanting vessel.
14, device according to claim 1 is characterized in that, a water inlet pipe is set on described decanting vessel, to keep adding water; The reflux pipe material of described decanting vessel connects the refluxing opening and the reactive system of lightness-removing column.
15, device according to claim 1 is characterized in that, described dehydration tower is packing tower or tray column.
16, device according to claim 1 is characterized in that, has 25-35 theoretical stage in the described dehydration tower.
17, device according to claim 1 is characterized in that, the cat head of described dehydration tower is provided with by the condenser of pipe connection and phlegma storage tank, and the phlegma pipeline of described phlegma storage tank connects the refluxing opening and the reactive system of dehydration tower.
18, device according to claim 1 is characterized in that, the methyl alcohol import on the described dehydration tower is arranged in the mid-way of dehydration tower profit reduction and reserving section.
19, device according to claim 1 is characterized in that, section is retained a percentage of the total profits for the enterprise's own use in the position of described methyl alcohol import in dehydration tower mid-way changes up and down in the scope of a theoretical stage.
20, device according to claim 1 is characterized in that, connects a tower bottom reboiler in described dehydration tower bottom.
21, device according to claim 1 is characterized in that, described weight-removing column has 30-45 theoretical stage.
22, device according to claim 1 is characterized in that, described weight-removing column has 35-45 theoretical stage.
23, device according to claim 1 is characterized in that, the cat head of described weight-removing column is provided with by the condenser of pipe connection and phlegma storage tank, and the phlegma pipeline of described phlegma storage tank connects the refluxing opening and the product extraction mouth of dehydration tower.
24, device according to claim 1 is characterized in that, connects a tower bottom reboiler in described weight-removing column bottom.
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| CN100575326C true CN100575326C (en) | 2009-12-30 |
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| US8575403B2 (en) | 2010-05-07 | 2013-11-05 | Celanese International Corporation | Hydrolysis of ethyl acetate in ethanol separation process |
| WO2012148509A1 (en) | 2011-04-26 | 2012-11-01 | Celanese International Corporation | Process for producing ethanol using a stacked bed reactor |
| US8710279B2 (en) | 2010-07-09 | 2014-04-29 | Celanese International Corporation | Hydrogenolysis of ethyl acetate in alcohol separation processes |
| US9024083B2 (en) | 2010-07-09 | 2015-05-05 | Celanese International Corporation | Process for the production of ethanol from an acetic acid feed and a recycled ethyl acetate feed |
| US8664454B2 (en) | 2010-07-09 | 2014-03-04 | Celanese International Corporation | Process for production of ethanol using a mixed feed using copper containing catalyst |
| US9272970B2 (en) | 2010-07-09 | 2016-03-01 | Celanese International Corporation | Hydrogenolysis of ethyl acetate in alcohol separation processes |
| US8754268B2 (en) | 2011-04-26 | 2014-06-17 | Celanese International Corporation | Process for removing water from alcohol mixtures |
| US9073816B2 (en) | 2011-04-26 | 2015-07-07 | Celanese International Corporation | Reducing ethyl acetate concentration in recycle streams for ethanol production processes |
| US8592635B2 (en) | 2011-04-26 | 2013-11-26 | Celanese International Corporation | Integrated ethanol production by extracting halides from acetic acid |
| US8895786B2 (en) | 2011-08-03 | 2014-11-25 | Celanese International Corporation | Processes for increasing alcohol production |
| US8686201B2 (en) | 2011-11-09 | 2014-04-01 | Celanese International Corporation | Integrated acid and alcohol production process having flashing to recover acid production catalyst |
| US8614359B2 (en) | 2011-11-09 | 2013-12-24 | Celanese International Corporation | Integrated acid and alcohol production process |
| CN103861310A (en) * | 2014-04-03 | 2014-06-18 | 泰兴市裕廊化工有限公司 | High-purity acetic acid rectification preparation system |
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