CN104447243A - Reactive distillation method and device for butyraldehyde synthesis by low-pressure carbonyl - Google Patents
Reactive distillation method and device for butyraldehyde synthesis by low-pressure carbonyl Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/009—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
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- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
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- C07C45/783—Separation; Purification; Stabilisation; Use of additives by gas-liquid treatment, e.g. by gas-liquid absorption
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Abstract
The invention relates to a reactive distillation method and device for butyraldehyde synthesis by low-pressure carbonyl. A gas phase outlet of a condenser at the top of a reactive distillation tower is connected with a lower feed port of an absorption tower, a liquid phase outlet is connected to a backflow feed port of the reactive distillation tower, and a tower bottom discharge material enters a flash tower; a flash tower bottom discharge material is a catalyst solution and is connected to a feed port in the upper part of a reaction section of the reactive distillation tower, and a tower top outlet is connected to an upper feed port of the absorption tower; waste gas is discharged from the top of the absorption tower, and a tower bottom discharge material is crude butyraldehyde and enters an upper feed port of a stripping tower; synthesis gas enters a bottom feed port of the stripping tower, a gas outlet in the top of the stripping tower is connected to a feed port of the reactive distillation tower, and a mixed butyraldehyde product is obtained after discharging from a tower kettle. The reaction of butyraldehyde synthesis by low-pressure carbonyl and butyraldehyde purification and distillation separation operated by two units are organically coupled in one device simultaneously, propylene in the condensed gas phase at the top of the reactive distillation tower is collected through operation of the absorption tower and the stripping tower, the recovery rate of propylene is up to 90%, and the quality purity of mixed butyraldehyde can be up to 99%.
Description
Technical field
The present invention relates to butyraldehyde production technical field, particularly relate to a kind of reactive distillation method and device of low pressure oxo process butyraldehyde.
Background technology
Butyraldehyde is the intermediate of important Organic Chemicals, is also the important source material of producing various fine chemical product.Butyraldehyde has butyraldehyde-n and isobutyric aldehyde 2 kinds of isomer, butyraldehyde-n mainly for the production of propyl carbinol and 2-Ethylhexyl Alcohol, also for the production of the fine chemical product such as TriMethylolPropane(TMP), polyvinyl butyral acetal; Isobutyric aldehyde is mainly for the production of isopropylcarbinol, neopentyl glycol, condensation and esterified prod 2,2,4-neopentyl glycol, isopropylformic acid, isopropyl cyanide etc.
The synthetic method of butyraldehyde is a lot, as: acetaldehyde condensation method, butanols oxydehydro process and oxo synthesis etc., wherein oxo synthesis is the main method of synthesis butyraldehyde.Oxo process butyraldehyde is that for raw material, reaction generates butyraldehyde in the presence of a catalyst with propylene and synthetic gas (consist of hydrogen and carbon monoxide and its mol ratio 1.02 ~ 1.04), then by distilling, butyraldehyde is separated into butyraldehyde-n and isobutyric aldehyde.The development experience of the carbonylic synthesis technology of propylene high pressure cobalt method, modified cobalt method and low pressure rhodium method, due to low pressure rhodium method there is low temperature, low pressure, the advantage such as speed of reaction is fast, side reaction is few, reduce investment outlay, be current most widely used technique.
CN1135475 discloses a kind of preparation method of aldehydes, it is characterized in that heating the liquid mixture flowed out in carbongl group synthesis reaction region, then it is supplied to gas-liquid contact tower top, the carbon monoxide entered with bottom and hydrogen counter current contact, to be separated and to reclaim unreacted alkene, and the unreacting olefin of recovery and carbon monoxide are resupplied to oxo process conversion zone together with hydrogen, tower reactor discharging obtains butyraldehyde product through separating catalyst.CN1133278A discloses a kind of preparation method of butyraldehyde, aldehyde distillation tower is run under adopting lower pressure condition, can obtain having and under relative high pressure condition with the aldehyde of the available substantially the same purity of ordinary method, wherein thermal load controls to low level, column bottom temperature can remain on low level, thus effectively can retrieve the heat dissipation in other step, and then reduce the consumption of energy.CN102115433A discloses a kind of method that ethene low pressure oxo process produces propionic aldehyde, and it is in feed stock conversion >=90% of ethene.Propionic aldehyde product content >=99.5, the method for its synthesis propionic aldehyde is equally applicable to butyraldehyde.
At present, have been reported the reaction and separation processes about propenecarbonyl synthesis butyraldehyde, realization rate first reacts in a kettle., reacted that after product must realize light constituent through high and low pressure tower, catalyzer is separated with product, obtain butyraldehyde product, catalyst solution is returned in reactor.Reaction rectification technique applies day by day a kind of process intensification technology simultaneously carried out in same equipment by simultaneous reaction and separation widely in chemical industry, both can save the investment of equipment, reduce again the expense of subsequent operations.The reaction rectification technique being applied in oxo process butyraldehyde aspect at present does not also have Patents and report.
Summary of the invention
The object of this invention is to provide a kind of reactive distillation method and device of low pressure oxo process butyraldehyde, use catalytic reaction rectification method provided by the invention, the advantage such as have that separation process scheme is simple, facility investment is lower, easy to operate and energy consumption is lower.
The reactive distillation method of low pressure oxo process butyraldehyde of the present invention and device, primarily of reactive distillation column, flashing tower, absorption tower and stripping tower composition, main products is butyraldehyde.The feature of method of the present invention and device is the employing of reaction rectification technique and equipment, being separated of light constituent and butyraldehyde is played carry out the low pressure carbongl group synthesis reaction of propylene at reactive distillation column while, the propylene in tower top light constituent can also be reclaimed by subsequent operations, realize making full use of of raw material.
Technical scheme of the present invention is as follows:
The reaction and rectification device of low pressure oxo process butyraldehyde of the present invention, comprises reactive distillation column, flashing tower, absorption tower, stripping tower, condenser, reboiler, compressor, pump and relevant feedstocks pipeline and the pipeline being connected above equipment; Reactive distillation column overhead arranges condenser, arranges reboiler at the bottom of tower; Reactive distillation column overhead condenser gaseous phase outlet is connected to the underfeed mouth on absorption tower, and liquid-phase outlet is connected to reactive distillation column reflux entry mouth, and discharging at the bottom of tower enters flashing tower; Discharging at the bottom of flashing tower tower is the opening for feed that catalyst solution is connected to reactive distillation column conversion zone top, and tower top outlet is connected to the opening for feed on the top on absorption tower; The tower top combustion gas on absorption tower, discharging at the bottom of tower is that cymogene aldehyde enters stripping tower upper feed inlet; Synthetic gas enters opening for feed at the bottom of stripping tower tower, and stripper overhead gas outlet is connected to reactive distillation column opening for feed, and tower reactor obtains mixing butyraldehyde product.
The reactive distillation method of low pressure oxo process butyraldehyde of the present invention is: raw material propylene (S01) enters the bottom of the conversion zone of reactive distillation column (T1), material synthesis gas (S02) part enters reactive distillation column (T1) conversion zone bottom, and a part of synthetic gas (S17) enters at the bottom of stripping tower tower; Reactive distillation column (T1) top gaseous phase (S03) enters reactive distillation column overhead condenser (E1), after condensation, gas phase (S04) enters the bottom of absorption tower (T3), after condensation, liquid phase (S05) total reflux is to reactive distillation column (T1), for mixing butyraldehyde and catalyst solution (S06) are as the charging of flashing tower (T2) at the bottom of reactive distillation column (T1) tower; Flashing tower (T2) tower top is enter pump (P2) pressurization after mixing butyraldehyde gas (S07) enters condenser (E3) condensation to obtain mixing the top that butyraldehyde liquid (S08) enters absorption tower (T3), be that catalyst solution (S09) enters condenser (E4) cooling at the bottom of flashing tower (T2) tower, then the solution (S10) after pump (P1) pressurization enter the top of reactive distillation column (T1) conversion zone; Absorption tower (T3) overhead gas (S13) goes to fuel section, and the cymogene aldehyde solution (S12) after extraction cymogene aldehyde (S11) at the bottom of tower enters pump (P3) pressurization enters the top of stripping tower (T4); Synthetic gas (S17) and cymogene aldehyde solution (S12) counter current contact in stripping tower (T4), the gas (S16) of overhead gas (S15) after compressor (C1) of stripping tower (T4) can return reactive distillation column (T1) charging as raw material, extraction mixing butyraldehyde product (S14) at the bottom of the tower of stripping tower (T4).
In the reactive distillation method of low pressure oxo process butyraldehyde: reactive distillation pressure tower 1.7-1.9Mpa, conversion zone temperature is 80-110 DEG C, catalyzer is rhodium-triphenylphosphine, solvent is the trimer of butyraldehyde, also butyraldehyde-n can be adopted to make solvent, in reaction solution, the massfraction of rhodium is 250-450ppm, and triphenylphosphine massfraction is 8-12%, and the mol ratio of feed composition propylene and synthetic gas is 1:2-1:3; Flashing tower pressure is 0.1-1Mpa; Absorption tower pressure is 0.1-1Mpa; Pressure of stripping tower is 0.1-3Mpa, and cymogene aldehyde solution and synthetic gas mol ratio are 1:1; Pressure all represents absolute pressure herein.
The reactive distillation method of low pressure oxo process butyraldehyde of the present invention and device, its advantage is the reaction of oxo process butyraldehyde and butyraldehyde purification rectifying separation two unit operations, organically be coupled in an equipment and carry out simultaneously, play being separated of light constituent and butyraldehyde simultaneously, both save facility investment, additionally reduce follow-up process cost.Can realize mixing being separated of butyraldehyde and catalyst solution by flashing tower.By the operation of absorption tower and stripping tower, can reclaim the propylene in gas phase after reactive distillation column overhead condensation, reach 90% to the rate of recovery of propylene, the quality purity of mixing butyraldehyde can reach 99%.
Accompanying drawing explanation
Fig. 1 is reactive distillation method and the device schematic diagram of low pressure oxo process butyraldehyde.
Equipment: T1. reactive distillation column, T2. flashing tower, T3. absorption tower, T4. stripping tower, P1. catalyst solution recycle pump, P2. flashing tower overhead extraction pump, extraction pump at the bottom of P3. absorbing tower, E1. reactive distillation column condenser, E2. reactive distillation column reboiler, E3. flashing tower tower top material condenser, E4. flashing tower materials at bottom of tower condenser, C1. compressor
Logistics: S01. raw material propylene, S02. material synthesis gas, S03. reactive distillation column overhead gas, S04. gas phase after reactive distillation column overhead condensation, S05. liquid phase after reactive distillation column overhead condensation, S06. butyraldehyde and catalyst solution is mixed, S07. butyraldehyde gas is mixed, S08. butyraldehyde liquid is mixed, S09. catalyst solution, S10. the catalyst solution after pump pressurization, S11. the cymogene aldehyde solution of extraction at the bottom of absorbing tower, S12. the cymogene aldehyde solution after pump pressurization, S13. absorption tower overhead gas, S14. butyraldehyde product is mixed, S15. stripper overhead gas, S16. the overhead gas after compressor, S17. the synthetic gas of admission stripper
Embodiment
Below in conjunction with accompanying drawing, method provided by the present invention and device are further detailed.
The present invention is achieved through the following technical solutions:
The reaction and rectification device of low pressure oxo process butyraldehyde, comprises reactive distillation column, flashing tower, absorption tower, stripping tower, condenser, reboiler, compressor, pump and relevant feedstocks pipeline and the pipeline being connected above equipment; Reactive distillation column overhead arranges condenser, arranges reboiler at the bottom of tower; Reactive distillation column overhead condenser gaseous phase outlet is connected to the underfeed mouth on absorption tower, and liquid-phase outlet is connected to reactive distillation column reflux entry mouth, and discharging at the bottom of tower enters flashing tower; Discharging at the bottom of flashing tower tower is the opening for feed that catalyst solution is connected to reactive distillation column conversion zone top, and tower top outlet is connected to the opening for feed on the top on absorption tower; The tower top combustion gas on absorption tower, discharging at the bottom of tower is that cymogene aldehyde enters stripping tower upper feed inlet; Synthetic gas enters opening for feed at the bottom of stripping tower tower, and stripper overhead gas outlet is connected to reactive distillation column opening for feed, and tower reactor obtains mixing butyraldehyde product.
The reactive distillation method of low pressure oxo process butyraldehyde of the present invention is: raw material propylene (S01) enters the bottom of the conversion zone of reactive distillation column (T1), material synthesis gas (S02) part enters reactive distillation column (T1) conversion zone bottom, and a part of synthetic gas (S17) enters at the bottom of stripping tower tower; Reactive distillation column (T1) top gaseous phase (S03) enters reactive distillation column overhead condenser (E1), after condensation, gas phase (S04) enters the bottom of absorption tower (T3), after condensation, liquid phase (S05) total reflux is to reactive distillation column (T1), for mixing butyraldehyde and catalyst solution (S06) are as the charging of flashing tower (T2) at the bottom of reactive distillation column (T1) tower; Flashing tower (T2) tower top is enter pump (P2) pressurization after mixing butyraldehyde gas (S07) enters condenser (E3) condensation to obtain mixing the top that butyraldehyde liquid (S08) enters absorption tower (T3), be that catalyst solution (S09) enters condenser (E4) cooling at the bottom of flashing tower (T2) tower, then the solution (S10) after pump (P1) pressurization enter the top of reactive distillation column (T1) conversion zone; Absorption tower (T3) overhead gas (S13) goes to fuel section, and the cymogene aldehyde solution (S12) after extraction cymogene aldehyde (S11) at the bottom of tower enters pump (P3) pressurization enters the top of stripping tower (T4); Synthetic gas (S17) and cymogene aldehyde solution (S12) counter current contact in stripping tower (T4), the gas (S16) of overhead gas (S15) after compressor (C1) of stripping tower (T4) can return reactive distillation column (T1) charging as raw material, extraction mixing butyraldehyde product (S14) at the bottom of the tower of stripping tower (T4).
Reactive distillation pressure tower 1.7-1.9Mpa in the reactive distillation method of low pressure oxo process butyraldehyde, conversion zone temperature is 80-110 DEG C, catalyzer is rhodium-triphenylphosphine, solvent is the trimer of butyraldehyde, also butyraldehyde-n can be adopted to make solvent, in reaction solution, the massfraction of rhodium is 250-450ppm, and triphenylphosphine massfraction is 8-12%, and the mol ratio of feed composition propylene and synthetic gas is 1:2-1:3; Flashing tower pressure is 0.1-1Mpa; Absorption tower pressure is 0.1-1Mpa; Pressure of stripping tower is 0.1-3Mpa, and cymogene aldehyde solution and synthetic gas mol ratio are 1:1.
Embodiment 1
In this example, reactive distillation pressure tower 1.7Mpa, conversion zone temperature is 110 DEG C, catalyzer is rhodium-triphenylphosphine, and solvent is the trimer of butyraldehyde, and in reaction solution, the massfraction of rhodium is 250ppm, triphenylphosphine massfraction is 8%, and the mol ratio of feed composition propylene and synthetic gas is 1:2; Flashing tower pressure is 1Mpa; Absorption tower pressure is 0.6Mpa; Pressure of stripping tower is 3Mpa, and cymogene aldehyde solution and synthetic gas mol ratio are 1:1.Final is 92% to the rate of recovery of propylene in reactive distillation column overhead non-condensable gas, and the quality purity of mixing butyraldehyde is 99%.
Embodiment 2
In this example, reactive distillation pressure tower 1.9Mpa, conversion zone temperature is 80 DEG C, catalyzer is rhodium-triphenylphosphine, and solvent is the trimer of butyraldehyde, and in reaction solution, the massfraction of rhodium is 350ppm, triphenylphosphine massfraction is 12%, and the mol ratio of feed composition propylene and synthetic gas is 1:3; Flashing tower pressure is 0.1Mpa; Absorption tower pressure is 1Mpa; Pressure of stripping tower is 0.1Mpa, and cymogene aldehyde solution and synthetic gas mol ratio are 1:1.Final is 93% to the rate of recovery of propylene in reactive distillation column overhead non-condensable gas, and the quality purity of mixing butyraldehyde is 99.5%.
Embodiment 3
In this example, reactive distillation pressure tower 1.8Mpa, conversion zone temperature is 100 DEG C, catalyzer is rhodium-triphenylphosphine, and solvent is the trimer of butyraldehyde, and in reaction solution, the massfraction of rhodium is 450ppm, triphenylphosphine massfraction is 10%, and the mol ratio of feed composition propylene and synthetic gas is 1:2.5; Flashing tower pressure is 0.5Mpa; Absorption tower pressure is 0.1Mpa; Pressure of stripping tower is 1Mpa, and cymogene aldehyde solution and synthetic gas mol ratio are 1:1.Final is 90% to the rate of recovery of propylene in reactive distillation column overhead non-condensable gas, and the quality purity of mixing butyraldehyde is 99.2%.
Claims (7)
1. a reaction and rectification device for low pressure oxo process butyraldehyde, comprises reactive distillation column, flashing tower, absorption tower, stripping tower, condenser, reboiler, compressor, pump and relevant feedstocks pipeline and the pipeline being connected above equipment; It is characterized in that reactive distillation column overhead arranges condenser, at the bottom of tower, reboiler is set; Reactive distillation column overhead condenser gaseous phase outlet is connected to the underfeed mouth on absorption tower, and liquid-phase outlet is connected to reactive distillation column reflux entry mouth, and discharging at the bottom of tower enters flashing tower; Discharging at the bottom of flashing tower tower is the opening for feed that catalyst solution is connected to reactive distillation column conversion zone top, and tower top outlet is connected to the opening for feed on the top on absorption tower; The tower top combustion gas on absorption tower, discharging at the bottom of tower is that cymogene aldehyde enters stripping tower upper feed inlet; Synthetic gas enters opening for feed at the bottom of stripping tower tower, and stripper overhead gas outlet is connected to reactive distillation column opening for feed, and tower reactor obtains mixing butyraldehyde product.
2. adopt the device of claim to carry out the reactive distillation method of low pressure oxo process butyraldehyde: to it is characterized in that raw material propylene enters the bottom of the conversion zone of reactive distillation column, a material synthesis gas part enters reactive distillation column conversion zone bottom, and a part of synthetic gas enters at the bottom of stripping tower tower; Reactive distillation column top gaseous phase enters reactive distillation column overhead condenser, and after condensation, gas phase enters the bottom on absorption tower, and after condensation, liquid phase total reflux is to reactive distillation column, is that mixing butyraldehyde and catalyst solution are as the charging of flashing tower at the bottom of reactive distillation column tower; Flashing tower tower top enters condenser for mixing butyraldehyde gas, enter pump pressurization after condensation to obtain mixing the top that butyraldehyde liquid enters absorption tower, be that catalyst solution enters condenser cooling at the bottom of flashing tower tower, then the solution after pump pressurization enter the top of reactive distillation column conversion zone; Absorption tower overhead gas goes to fuel section, and the cymogene aldehyde solution after extraction cymogene aldehyde at the bottom of tower enters pump pressurization enters the top of stripping tower; Synthetic gas and cymogene aldehyde solution counter current contact in stripping tower, the gas of overhead gas after compressor of stripping tower returns reactive distillation column charging as raw material, extraction mixing butyraldehyde product at the bottom of the tower of stripping tower.
3. method as claimed in claim 2, it is characterized in that reactive distillation pressure tower 1.7-1.9Mpa, conversion zone temperature is 80-110 DEG C.
4. method as claimed in claim 2, is characterized in that. catalyzer is rhodium-triphenylphosphine, and solvent is the trimer of butyraldehyde; Or adopting butyraldehyde-n to make solvent, in reaction solution, the massfraction of rhodium is 250-450ppm, and triphenylphosphine massfraction is 8-12%, and the mol ratio of feed composition propylene and synthetic gas is 1:2-1:3.
5. method as claimed in claim 2, is characterized in that flashing tower pressure is 0.1-1Mpa.
6. method as claimed in claim 2, is characterized in that absorption tower pressure is 0.1-1Mpa.
7. method as claimed in claim 2, it is characterized in that pressure of stripping tower is 0.1-3Mpa, cymogene aldehyde solution and synthetic gas mol ratio are 1:1.
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| CN107011144A (en) * | 2017-05-27 | 2017-08-04 | 天津渤化永利化工股份有限公司 | The utilization system and method for off-gas in industrial propenecarbonyl synthesizer |
| CN109071396A (en) * | 2016-04-21 | 2018-12-21 | 庄信万丰戴维科技有限公司 | Method |
| CN111440054A (en) * | 2020-04-02 | 2020-07-24 | 北京诺维新材科技有限公司 | Preparation method and preparation device of butyraldehyde |
| CN112675665A (en) * | 2020-12-16 | 2021-04-20 | 万华化学集团股份有限公司 | Method and device for separating oxo-synthesis tail gas |
| CN112728870A (en) * | 2021-01-26 | 2021-04-30 | 上海寰球工程有限公司 | Ethylene recovery system and process for preparing n-propionaldehyde and n-propanol from ethylene |
| CN113214058A (en) * | 2021-05-08 | 2021-08-06 | 中石油吉林化工工程有限公司 | Method and equipment for producing propionaldehyde by ethylene hydroformylation liquid phase circulation |
| CN114728870A (en) * | 2019-11-07 | 2022-07-08 | 伊士曼化工公司 | Recovery of the constituent oxo diols |
| CN116212771A (en) * | 2023-03-09 | 2023-06-06 | 宁波巨化化工科技有限公司 | Liquid phase single reaction kettle capable of circularly reacting to improve overall yield |
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| CN109071396A (en) * | 2016-04-21 | 2018-12-21 | 庄信万丰戴维科技有限公司 | Method |
| CN109071396B (en) * | 2016-04-21 | 2022-06-24 | 庄信万丰戴维科技有限公司 | Process for separating linear and branched aldehydes |
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| CN112728870A (en) * | 2021-01-26 | 2021-04-30 | 上海寰球工程有限公司 | Ethylene recovery system and process for preparing n-propionaldehyde and n-propanol from ethylene |
| CN113214058A (en) * | 2021-05-08 | 2021-08-06 | 中石油吉林化工工程有限公司 | Method and equipment for producing propionaldehyde by ethylene hydroformylation liquid phase circulation |
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