CN201525813U - Acetic acid synthesizer utilizing methanol carbonylation - Google Patents
Acetic acid synthesizer utilizing methanol carbonylation Download PDFInfo
- Publication number
- CN201525813U CN201525813U CN2009202186989U CN200920218698U CN201525813U CN 201525813 U CN201525813 U CN 201525813U CN 2009202186989 U CN2009202186989 U CN 2009202186989U CN 200920218698 U CN200920218698 U CN 200920218698U CN 201525813 U CN201525813 U CN 201525813U
- Authority
- CN
- China
- Prior art keywords
- acetic acid
- methyl iodide
- reactor
- tower
- evaporator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses an acetic acid synthesizer utilizing methanol carbonylation, which comprises a reactor, a refining device, a scrubbing tower, a methyl iodide circulation tower and an evaporator, wherein a side extraction outlet of the reactor is connected to the methyl iodide circulation tower, a top outlet of the methyl iodide circulation tower is connected with the reactor, a side extraction outlet of the methyl iodide circulation tower is connected with the evaporator, a gas outlet at the top of the evaporator is connected to the refining device, and an outlet at the bottom of the evaporator is connected back to the reactor. The synthesizer utilizes carbonylation catalyzed by rhodium to generate acetic acid. By arranging the methyl iodide circulation tower and the evaporator in front of refining device, methyl iodide circulates in the reaction system, thereby reducing methyl iodide impurity content mixed in acetic acid and simultaneously saving energy consumption needed for purifying acetic acid.
Description
Technical field
The utility model relates to a kind of acetic acid synthesized device, particularly utilizes the device of methanol carbonyl synthesized acetic acid.
Background technology
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.After having developed the production technique of acetic acid synthesized by low pressure methanol carbonylation since the U.S. Monsanto Company sixties in last century, the acetic acid synthesized by low pressure methanol carbonylation technology becomes the main method of producing acetic acid in the world at present.
Consult Fig. 1, the production equipment of acetic acid synthesized by low pressure methanol carbonylation mainly comprises reactor 1, four towers of refining plant (lightness-removing column 2, dehydration tower 3, weight-removing column 4, waste acid column 5), and scrubbing tower 6, rectifying tower phlegma backflash 7.Methyl alcohol and carbon monoxide, catalyzer etc. add reactor 1 bottom, 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 plant with gas phase, deviates from lighting end, and the gas of cat head enters scrubbing tower through 7 of distillation tower phlegma backflashes.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.Three towers and reactor 1 expellant gas gather, with burning emptying behind the cold methanol washing and recycling iodine.
Technical process of low pressure methanol carbonylation method and device are all being updated, and improve constantly, and have advantageously promoted the raising of maximization, energy consumption reduction, cost decline and the competitive power of production equipment.The purification schemes of company's Dichlorodiphenyl Acetates such as BP, contest road has been done research, has carried out the improvement of purifying technique.The change that the technology that adopts single rectification zone is come catalyzer in the adaptive response liquid has been explained by BP company in the patent application CN93108283 of China; And contest road company controls the stratified temperature of decanting vessel and add water transformation acetic acid purification schemes in material at first distillation tower in the patent application CN96190401 of China.Disclose in the CN96190401 patent application behind the cat head vapor condensation of lightness-removing column decanting vessel is set, so that isolate gas phase at decanting vessel behind the cat head vapor condensation, isolated 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.Because the severe corrosive of iodide, high score are from energy consumption, in recent years, the separation problem of iodide became the improved important step of methanol carbonyl synthesized acetic acid device in the whole acetic acid synthesis system.
The utility model content
Technical problem to be solved in the utility model provides in the presence of the catalyzer that contains the 8th family's metal by methyl alcohol is carried out the device that carbonylation prepares acetic acid, particularly generate the device of acetic acid by the catalytic carbonylation reaction of rhodium, this device is by being provided with methyl iodide recycle column and vaporizer before rectifier unit, methyl iodide is circulated at reactive system, reduced the amount of sneaking into methyl iodide impurity in the acetic acid, the rhodium catalyst of carrying secretly in efficient recovery iodide ion and the flash steam has been saved the required energy consumption of purifying acetic acid simultaneously.
For solving the problems of the technologies described above, technical solution adopted in the utility model is, a kind of methanol carbonyl synthesized acetic acid device, this device mainly comprises reactor, refining plant and scrubbing tower, described device also comprises methyl iodide recycle column and vaporizer, described reactor-side extraction material outlet connects the methyl iodide recycle column, described methyl iodide recycle column tower top outlet ligation device, the outlet of methyl iodide recycle column side extraction material connects vaporizer, the pneumatic outlet at vaporizer top is connected to refining plant, and the outlet of base of evaporator is returned and is connected to reactor.
Wherein, described methyl iodide recycle column has a power set; The CO raw material pipeline of described reactor also is connected to methyl iodide recycle column bottom and power set respectively; Described power set is an injector; Described vaporizer is a tower evaporator; The stage number of described tower evaporator is four to 20; Described refining plant also comprises the phlegma backflash; Described vaporizer has the washing composition inlet; Described washing composition inlet links to each other with refining plant phlegma backflash.
The beneficial effect that the utility model can reach is:
1. the methyl iodide recycle column is separated Returning reactor to the part lower boiling methyl iodide in the reactor-side extraction material in the utility model device, reduced the amount of the methyl iodide that enters refining plant, and can effectively solve iodine corrosive problem in the follow up device, guarantee the steady running of system.
2. acetic acid synthesis from methanol carbonylation device of the present utility model, by technical process correspondingly, the promotor methyl iodide need not to use at whole device internal recycle, has saved the needed energy consumption of purifying acetic acid.
3. iodine consumption has also dropped to minimumly in the acetic acid synthesized process of the utility model device, has effectively reduced the content of iodine impurity in the finished product acetic acid.
4. tower evaporator is set in the utility model device can fully be reclaimed rhodium catalyst, detergent washing is thorough, and the washing composition consumption is few, the loss of rhodium catalyst is few, and can separate hydrogen iodide well, and reduced the purifying energy consumption of follow-up refining plant, guaranteed the lower iodine content of finished product acetic acid, the load of lightness-removing column is reduced, thereby the reduction steam consumption, because hydrogen iodide content reduces, the diluted acid amount of returning of washing hydrogen iodide is reduced.
Description of drawings
Fig. 1 is the device synoptic diagram that low pressure methanol carbonylation that existing Monsanto Company takes is produced acetic acid.
Fig. 2 is the utility model methanol carbonyl synthesized acetic acid device synoptic diagram.
Major label description in figure:
1 is reactor; 2 is lightness-removing column; 3 is dehydration tower; 4 is weight-removing column; 5 is waste acid column; 6 is scrubbing tower; 7 is distillation tower phlegma backflash; 8 is the methyl iodide recycle column; 9 is injector; 10 is tower evaporator.
Embodiment
Below in conjunction with Fig. 2 the utility model methanol carbonyl synthesized acetic acid device synoptic diagram the utility model is described in further detail.
The utility model embodiment methanol carbonyl synthesized acetic acid dress is compared with existing apparatus, mainly is to be provided with methyl iodide recycle column 8 and tower evaporator 10 between reactor 1 and refining plant.Reactor 1 side extraction material outlet 11 connects methyl iodide recycle column 8 inlets 81, methyl iodide recycle column 8 side extraction material outlet 82 connects tower evaporator 10 inlets 101, tower evaporator 10 top gas outlet 102 is connected to refining plant, and tower evaporator 10 outlet at bottoms are connected to reactor 1 103 times.Methyl iodide recycle column 8 tower top outlets 83 are provided with injector 9 simultaneously, be used for methyl iodide recycle column 8 isolating methyl iodide are back to reactor 1, the CO raw material pipeline of reactor 1 also is connected to methyl iodide recycle column bottom inlet 84 and injector 9, carries the power gas of promotor methyl iodide as gas.Wherein, the stage number of tower evaporator 10 is four to 20, is provided with ten in the present embodiment, and the washing composition of tower evaporator 10 is from the diluted acid of the distillation tower phlegma backflash 7 of refining plant.
The device of using the utility model embodiment mainly contains following processing step and improves utilizing in the technology of acetic acid synthesis from methanol carbonylation as catalyzer with rhodium:
(1) the thick acetic acid that comes out of reactor-side extraction material is introduced into the methyl iodide recycle column, utilizes the methyl iodide recycle column to isolate the lower boiling methyl iodide, and injector provides power for the methyl iodide Returning reactor, and raw material CO is as the gas stripping gas body of this power.
(2) methyl iodide recycle column side extraction material enters tower evaporator, and thorough washing reclaims rhodium catalyst and the hydrogen iodide of carrying secretly in the flash distillation vapour phase, returns with mother liquor then, and gas phase enters refining plant.
Like this, the methyl iodide of quite a few is in the reactor cycles utilization, and the content of the hydrogen iodide in the refining system also reduces greatly, and rhodium consumption and steam consumption all significantly reduce, and have saved cost.
To sum up institute is old, only is the preferred embodiment of the utility model, is not the scope that is used for limiting the utility model enforcement.Be that all equalizations of being done according to the utility model claim change and modification, be all the utility model claim and contain.
Claims (9)
1. methanol carbonyl synthesized acetic acid device, this device mainly comprises reactor, refining plant and scrubbing tower, it is characterized in that, described device also comprises methyl iodide recycle column and vaporizer, described reactor-side extraction material outlet connects the methyl iodide recycle column, described methyl iodide recycle column tower top outlet ligation device, and the outlet of methyl iodide recycle column side extraction material connects vaporizer, the pneumatic outlet at vaporizer top is connected to refining plant, and the outlet of base of evaporator is returned and is connected to reactor.
2. methanol carbonyl synthesized acetic acid device according to claim 1 is characterized in that, described methyl iodide recycle column has a power set.
3. methanol carbonyl synthesized acetic acid device according to claim 2 is characterized in that, the CO raw material pipeline of described reactor also is connected to methyl iodide recycle column bottom and power set respectively.
4. according to claim 2 or 3 described methanol carbonyl synthesized acetic acid devices, it is characterized in that described power set is an injector.
5. methanol carbonyl synthesized acetic acid device according to claim 1 and 2 is characterized in that, described vaporizer is a tower evaporator.
6. methanol carbonyl synthesized acetic acid device according to claim 5 is characterized in that, the stage number of described tower evaporator is four to 20.
7. methanol carbonyl synthesized acetic acid device according to claim 1 and 2 is characterized in that described refining plant also comprises the phlegma backflash.
8. methanol carbonyl synthesized acetic acid device according to claim 7 is characterized in that, described vaporizer has the washing composition inlet.
9. methanol carbonyl synthesized acetic acid device according to claim 8 is characterized in that, described washing composition inlet links to each other with the phlegma backflash of refining plant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202186989U CN201525813U (en) | 2009-10-16 | 2009-10-16 | Acetic acid synthesizer utilizing methanol carbonylation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202186989U CN201525813U (en) | 2009-10-16 | 2009-10-16 | Acetic acid synthesizer utilizing methanol carbonylation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201525813U true CN201525813U (en) | 2010-07-14 |
Family
ID=42517106
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009202186989U Expired - Lifetime CN201525813U (en) | 2009-10-16 | 2009-10-16 | Acetic acid synthesizer utilizing methanol carbonylation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201525813U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106110696A (en) * | 2016-08-04 | 2016-11-16 | 兖矿水煤浆气化及煤化工国家工程研究中心有限公司 | The multifunctional evaporating equipment separated for thick product in oxo process class commercial plant |
| CN113480422A (en) * | 2021-06-29 | 2021-10-08 | 煜格（北京）科技有限公司 | Production method for acetic acid and propionic acid single production or joint production |
-
2009
- 2009-10-16 CN CN2009202186989U patent/CN201525813U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106110696A (en) * | 2016-08-04 | 2016-11-16 | 兖矿水煤浆气化及煤化工国家工程研究中心有限公司 | The multifunctional evaporating equipment separated for thick product in oxo process class commercial plant |
| CN106110696B (en) * | 2016-08-04 | 2018-10-16 | 兖矿水煤浆气化及煤化工国家工程研究中心有限公司 | Multifunctional evaporating equipment in carbonylation synthesis class commercial plant for crude product separation |
| CN113480422A (en) * | 2021-06-29 | 2021-10-08 | 煜格（北京）科技有限公司 | Production method for acetic acid and propionic acid single production or joint production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2021047391A1 (en) | Method for synthesizing acetic acid by low-pressure methanol carbonylation | |
| CN101481307B (en) | Method for separating acetic acid and sec-butyl acetate from reaction products | |
| CN103012062A (en) | Process for indirectly producing alcohol with synthetic gas and application of process | |
| CN101429098B (en) | Method for synthesis of methanol with CO, CO2 and H#[-2] | |
| CN206232628U (en) | A kind of production system of cyclohexanone | |
| CN106588536A (en) | Preparation method and preparation system of cyclohexanone | |
| CN205188178U (en) | Methyl nitrite's regenerating unit system in synthetic gas system ethylene glycol technology | |
| CN106631684A (en) | Method for preparing SBA(sec-butyl alcohol) through hydrolysis with sec-butyl acetate | |
| CN105111079A (en) | Method and device for separating acetic acid sec-butyl ester and sec-butyl alcohol | |
| CN101376630B (en) | Intermittent reaction rectification method and apparatus for synthesizing methyl formate | |
| CN103242158B (en) | Technological method for synthesizing ethyl acetate | |
| CN205188177U (en) | Methyl nitrite's regenerating unit system in synthetic gas system ethylene glycol technology | |
| CN104370740A (en) | Production method of isobornyl acetate | |
| CN105461515A (en) | Method for preparing cyclopentanol from cyclopentene | |
| CN201525813U (en) | Acetic acid synthesizer utilizing methanol carbonylation | |
| CN108947774A (en) | A kind of method and device of separating isopropanol | |
| CN103588618A (en) | Reactive distillation method and device for producing ethanol from methyl acetate by adding hydrogen | |
| CN203602526U (en) | Reactive distillation device for producing ethanol from methyl acetate by adding hydrogen | |
| CN203007176U (en) | Alcoholysis device system for preparing dioctyl terephthalate from Dacron wastes | |
| CN203513535U (en) | Production device of synthesized methyl tertiary butyl ether | |
| CN205740823U (en) | A kind of MTP device | |
| CN201988374U (en) | Tower type esterification apparatus for synthesizing linalyl acetate | |
| CN204939338U (en) | A kind of reactive system of coking crude benzene hydrogenation technique | |
| CN201524434U (en) | Integrated evaporator for carbonylation acetic acid technology | |
| CN101967080A (en) | Method for refining methane chloride crude product |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20100714 |