CN107032953B - Device and conversion method suitable for octanol and butanol conversion production - Google Patents
Device and conversion method suitable for octanol and butanol conversion production Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
- C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
- C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
- C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/17—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by hydrogenation of carbon-to-carbon double or triple bonds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/61—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups
- C07C45/67—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton
- C07C45/68—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms
- C07C45/72—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reactions not involving the formation of >C = O groups by isomerisation; by change of size of the carbon skeleton by increase in the number of carbon atoms by reaction of compounds containing >C = O groups with the same or other compounds containing >C = O groups
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Abstract
The invention relates to a device and a conversion method suitable for octanol and butanol conversion production, wherein the device comprises a condensation system, a hydrogenation system, a pre-rectification system and a rectification system, the hydrogenation system comprises a hydrogenation evaporator and a hydrogenation reactor, the pre-rectification system comprises a pre-rectification tower, a pre-rectification tower condenser and a pre-rectification tower vacuum system, the rectification system comprises a rectification tower, a rectification tower condenser and a rectification tower vacuum system, an octenal feeding pipeline is arranged between the condensation system and the hydrogenation evaporator, the octenal feeding pipeline is communicated with an n-butyraldehyde feeding pipeline, the pre-rectification tower vacuum pipeline is communicated with a pre-rectification tower low-pressure nitrogen pipeline and a pre-rectification tower to-flare pipeline, and the rectification tower vacuum pipeline is communicated with a rectification tower low-pressure nitrogen pipeline and a rectification tower to-flare pipeline. The invention adopts a mode of adding a plurality of pipelines and valve control to realize the mutual switching of the octanol production device and the butanol production device, thereby increasing the applicability of the whole device, saving the equipment investment and reducing the occupied area.
Description
Technical Field
The invention relates to a device and a conversion method suitable for conversion production of octanol and butanol.
Background
Octanol and butanol are important basic raw materials for chemical production, and are mainly used for preparing phthalic acid esters and aliphatic dibasic acid ester plasticizers, such as dioctyl phthalate, dioctyl azelate, dioctyl sebacate and the like, and are respectively used as main plasticizers and cold-resistant auxiliary plasticizers, defoamers, dispersants, mineral processing agents and petroleum additives for plastics, and are also used for printing and dyeing, paint, films and the like, and butanol is mainly used for preparing n-butyl ester plasticizers of phthalic acid, aliphatic dibasic acid and phosphoric acid, and is widely used for preparing raw materials of butyraldehyde, butyric acid, butylamine, butyl lactate and the like in various plastics and rubber products in organic synthesis.
In recent years, with the rapid development of the chemical industry, butanol and octanol yields and consumption are rapidly increasing. The traditional industrial preparation method of octanol is that n-butyraldehyde is subjected to self-condensation to produce octenal, the octenal is hydrogenated to produce octanol, and a production device consists of a condensation unit, a hydrogenation unit and a rectification unit. The traditional industrial preparation method of butanol is that n-butyraldehyde is hydrogenated to generate butanol, and a production device consists of a hydrogenation unit and a rectification unit. The butanol production device does not need a condensation unit, the rectification system adopts micro-positive pressure rectification, the octanol rectification system adopts vacuum rectification, and the production device of the butanol and the octanol rectification system cannot be commonly used.
For example, chinese patent (CN 104557457 a) discloses a reactive distillation method and apparatus for producing butanol from butyraldehyde, comprising an evaporator, a reactive distillation column, a butanol distillation column, an n-isobutanol separation column, a condenser, a reboiler, a compressor, a pump, and related feed lines and lines connecting the above devices; the method and the device are characterized in that the adoption of the reaction rectification technology and equipment can separate light components from the top of the tower when the butyraldehyde hydrogenation reaction is carried out in the reaction rectification tower, normal butanol and isobutanol can be obtained through subsequent separation, two unit operations of butyraldehyde production butanol and purification rectification separation are coupled in one equipment to be carried out simultaneously, and the reaction products are purified simultaneously after the reaction is finished, so that the equipment investment is saved and the subsequent operation cost is reduced. The mass purity of the n-butanol obtained after the separation of the subsequent butanol rectifying tower and the n-isobutanol separating tower can reach 99.5%, and the mass purity of the isobutanol can reach 99%.
As another example, chinese patent (CN 203494194U) discloses an octanol rectifying device, which comprises an octanol rectifying tower, a condenser, a reflux tank, a reflux pump, an octanol storage tank, a superconducting pipe, heat conducting oil, a vacuum pump, and a conduit. And (3) vacuumizing by a vacuum pump, introducing octenal tower residual liquid into an octanol rectifying tower, heating by heat conduction oil and conducting heat by a superconducting pipe to enable the octenal tower residual liquid to be changed into gas, condensing the gas by a condenser, enabling condensate to enter a reflux tank, enabling most of liquid to return to the top of the octanol rectifying tower by the reflux pump, and enabling cooled octanol to enter an octanol storage tank. The octanol rectifying device saves energy, protects environment and improves economic benefit.
The two above Chinese patents are improved on the production device of butanol and octanol respectively, but are only applicable to single products, and the flexibility is poor.
Disclosure of Invention
The invention aims to solve the technical problems that the existing butanol and octanol production device is only suitable for single octanol or butanol products, cannot be used universally and has poor flexibility, and provides a device and a conversion method suitable for octanol and butanol conversion production.
The technical scheme adopted by the invention for solving the technical problems is as follows: the utility model provides a device suitable for octanol and butanol conversion production, including condensation system, hydrogenation system, pre-rectification system and rectification system, hydrogenation system includes the hydrogenation evaporator, hydrogenation reactor, pre-rectification system includes the pre-rectification tower, pre-rectification tower condenser and pre-rectification tower vacuum system, rectification system includes the rectifying column, rectifying column condenser and rectifying column vacuum system, be equipped with the octenal feed line between condensation system and the hydrogenation evaporator, the intercommunication has normal butyraldehyde feed line on the octenal feed line, connect through pre-rectification tower vacuum line between pre-rectification tower condenser and the pre-rectification tower vacuum system, the intercommunication has pre-rectification tower low pressure nitrogen line and pre-rectification tower to the torch pipeline on the pre-rectification tower vacuum line, connect through rectifying tower vacuum line between rectifying tower condenser and the rectifying tower vacuum system, the intercommunication has rectifying tower low pressure nitrogen line and rectifying tower to the torch pipeline on the rectifying tower vacuum line.
In the technical scheme, preferably, the hydrogenation system further comprises a hydrogenation feed heater, a hydrogenation reactor, a hydrogenation circulating compressor, a hydrogenation heat exchanger, a hydrogenation condenser and a hydrogenation gas-liquid separator, wherein a crude hydrogenation product pipeline is arranged at the lower end of the hydrogenation gas-liquid separator.
Preferably, the pre-rectifying system further comprises a pre-rectifying tower bottom reboiler, a pre-rectifying tower pressure controller, a pre-rectifying tower reflux tank, a pre-rectifying tower reflux pump and a pre-rectifying tower kettle pump, wherein the pre-rectifying tower pressure control pipeline is connected with a pre-rectifying tower low-pressure nitrogen pipeline and a pre-rectifying tower forward flare pipeline respectively, and a product pipeline for removing light components is connected to the bottom of the pre-rectifying tower.
Preferably, the rectifying system further comprises a rectifying tower bottom reboiler, a rectifying tower pressure controller, a rectifying tower reflux tank, a rectifying tower reflux pump and a rectifying tower kettle pump, wherein the rectifying tower pressure control pipeline is connected with a rectifying tower low-pressure nitrogen pipeline and a rectifying tower to-flare pipeline respectively, the product pipeline is connected with the rectifying tower reflux pump, and the tower kettle heavy component pipeline is connected to the bottom of the rectifying tower.
The process for converting from octanol production to butanol production is as follows:
(1) Stopping octenal feed;
(2) Completely evaporating octenal in the hydrogenation evaporator, and completely discharging the crude octanol into a rectification system under the action of pressure;
(3) The pre-rectifying system and the rectifying system continue to operate, and the tower bottom of the pre-rectifying tower and the tower bottom of the rectifying tower are reduced to low liquid level;
(4) Purging the hydrogenation system, the pre-rectification system and the materials in the rectification system to an intermediate tank area by using nitrogen, and comprehensively replacing the materials in the device until octanol does not exist in the system;
(5) Cutting off a vacuum pipeline of the pre-rectifying tower, and opening a low-pressure nitrogen pipeline of the pre-rectifying tower and a flare pipeline of the pre-rectifying tower;
(6) Cutting off a vacuum pipeline of the rectifying tower, and opening a low-pressure nitrogen pipeline of the rectifying tower and a flare pipeline of the rectifying tower;
(7) Regulating the internal of the pre-rectification and rectification system to be in a constant micro-positive pressure state;
(8) The n-butyraldehyde feed was started.
A method for converting butanol production to octanol production, comprising:
(1) Stopping feeding the n-butyraldehyde;
(2) Completely evaporating butyraldehyde in the hydrogenation evaporator, and completely discharging crude butanol into a rectification system under the action of pressure;
(3) The pre-rectifying system and the rectifying system continue to operate, and the tower bottom of the pre-rectifying tower and the tower bottom of the rectifying tower are reduced to low liquid level;
(4) Purging the hydrogenation system, the pre-rectification system and materials in the rectification system to an intermediate tank area by using nitrogen, and comprehensively replacing the materials in the device until no butanol exists in the system;
(5) Cutting off a low-pressure nitrogen pipeline of the pre-rectifying tower and a flare pipeline of the pre-rectifying tower, and opening a vacuum pipeline of the pre-rectifying tower;
(6) Cutting off a low-pressure nitrogen pipeline of the rectifying tower and a flare pipeline which is sent to the rectifying tower, and opening a vacuum pipeline of the rectifying tower;
(7) Vacuumizing the pre-rectification and rectification system;
(8) The octenal feed was started.
According to the invention, the butyraldehyde feeding pipeline from the tank area is added on the octenal feeding pipeline of the hydrogenation evaporator, and the n-butyraldehyde can enter the hydrogenation system from the pipeline, so that the hydrogenation system can be used for hydrogenating octenal and also can be used for hydrogenating butyraldehyde, the applicability of the hydrogenation system is improved, and the equipment investment is saved.
In the invention, a low-pressure nitrogen pipeline of the pre-rectifying tower and a pipeline of the pre-rectifying tower which is connected to a torch are added on a vacuum pipeline of the pre-rectifying tower in the pre-rectifying system, so that the pre-rectifying system can be used for pre-rectifying crude octanol and pre-rectifying crude butanol, the applicability of the pre-rectifying system is improved, and the equipment investment is saved.
In the invention, the low-pressure nitrogen pipeline of the rectifying tower and the pipeline of the rectifying tower which is connected to the torch are added on the vacuum pipeline of the rectifying tower in the rectifying system, and the rectifying system can be used for rectifying the octanol product for removing the light components and the butanol product for removing the light components, thereby increasing the applicability of the rectifying system and saving the equipment investment.
According to the invention, a series of simple operations and valve control are performed on the premise that the device is not changed, so that the mutual switching between the octanol production device and the butanol production device can be realized according to the market demand of octanol and butanol, the applicability of the whole device is increased, the device cost of a chemical plant is reduced, and the occupied area is reduced.
Drawings
The invention will be further described with reference to the drawings and examples.
FIG. 1 is a schematic diagram of the hydrogenation system architecture of the apparatus for conversion production of octanol and butanol according to the present invention.
FIG. 2 is a schematic diagram of the structure of the pre-rectification system of the apparatus for conversion production of octanol and butanol according to the present invention.
FIG. 3 is a schematic diagram of the rectification system of the apparatus for the conversion production of octanol and butanol according to the present invention.
In the accompanying drawings:
1. condensation system 2, hydrogenation evaporator 3, hydrogenation feed heater
4. Hydrogenation reactor 5, hydrogenation circulation compressor 6 and hydrogenation heat exchanger
7. Hydrogenation condenser 8, hydrogen adding liquid separator 9 and octenal feeding pipeline
91. Octenal stop valve 10, n-butyraldehyde feed line 101, n-butyraldehyde stop valve
11. Hydrogen line 111, hydrogen shut-off valve 12, crude hydrogenation product line
13. Prefractionation column 14, prefractionation column bottom reboiler 15, prefractionation column condenser
16. Prestartion tower pressure controller 17, prestartion tower vacuum system 18, prestartion tower reflux drum
19. Prefractionation column reflux pump 20, prefractionation column tank pump 21, prefractionation column vacuum line
211. Pre-rectifying column vacuum pipeline stop valve 22, pre-rectifying column pressure control pipeline 23 and pre-rectifying column low-pressure nitrogen pipeline
231. The first pressure regulating valve 232 of the pre-rectifying tower, the low-pressure nitrogen stop valve 24 of the pre-rectifying tower and the pre-rectifying tower are connected to a flare pipeline
241. Second pressure regulating valve 242 of pre-rectifying tower, product pipeline of the pre-rectifying tower going to torch stop valve 25 and removing light components
26. Rectifying column 27, rectifying column bottom reboiler 28, rectifying column condenser
29. Rectifying column pressure controller 30, rectifying column vacuum system 31, rectifying column reflux drum
32. Rectifying column reflux pump 33, rectifying column bottom pump 34, rectifying column vacuum pipeline
341. Rectifying column vacuum line stop valve 35, rectifying column pressure control line 36, rectifying column low pressure nitrogen line
361. First pressure regulating valve 362 of rectifying column, low-pressure nitrogen stop valve 37 of rectifying column, and flare line for rectifying column
371. Second pressure regulating valve 372 of rectifying tower, heavy component pipeline of rectifying tower to torch stop valve 38 and tower kettle
39. Product pipeline
Detailed Description
The present invention will be described in further detail with reference to the following examples in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
[ example ]:
1-3, a device suitable for conversion production of octanol and butanol comprises a condensation system 1, a hydrogenation system, a pre-rectification system and a rectification system.
The hydrogenation system comprises a hydrogenation evaporator 2, a hydrogenation feeding heater 3, a hydrogenation reactor 4, a hydrogenation circulating compressor 5, a hydrogenation heat exchanger 6, a hydrogenation condenser 7 and a hydrogenation gas-liquid separator 8, wherein an octenal feeding pipeline 9 is arranged between the condensation system 1 and the hydrogenation evaporator 2, an octenal stop valve 91 is arranged on the octenal feeding pipeline 9 and positioned on the right side of the octenal stop valve 91, a n-butyraldehyde feeding pipeline 10 is communicated with the octenal feeding pipeline 9, a n-butyraldehyde stop valve 101 is arranged on the n-butyraldehyde feeding pipeline 10, the other end of the n-butyraldehyde feeding pipeline 10 is communicated with a tank area, a hydrogen pipeline 11 is communicated with the pipeline between the hydrogenation circulating compressor 5 and the hydrogenation heat exchanger 6, a hydrogen stop valve 111 is arranged on the hydrogen pipeline 11, a crude hydrogenation product pipeline 12 is arranged at the lower end of the hydrogenation gas-liquid separator 8, and the crude hydrogenation product pipeline 12 is used for conveying a crude hydrogenation product to a pre-rectification system and is connected with a pre-rectification tower 13 and positioned in a position on the middle part of the pre-rectification tower 13.
The pre-rectifying system comprises a pre-rectifying tower 13, a pre-rectifying tower bottom reboiler 14, a pre-rectifying tower condenser 15, a pre-rectifying tower pressure controller 16, a pre-rectifying tower vacuum system 17, a pre-rectifying tower reflux tank 18, a pre-rectifying tower reflux pump 19 and a pre-rectifying tower bottom pump 20.
The pre-rectifying tower condenser 15 is connected with the pre-rectifying tower vacuum system 17 through a pre-rectifying tower vacuum pipeline 21, a pre-rectifying tower vacuum pipeline stop valve 211 is arranged on the pre-rectifying tower vacuum pipeline 21, two branches are communicated with the pre-rectifying tower vacuum pipeline 21, a pre-rectifying tower low-pressure nitrogen pipeline 23 and a pre-rectifying tower forward-to-flare pipeline 24 are respectively arranged on the pre-rectifying tower low-pressure nitrogen pipeline 23, a pre-rectifying tower first pressure regulating valve 231 and a pre-rectifying tower low-pressure nitrogen stop valve 232 are respectively arranged on the pre-rectifying tower forward-to-flare pipeline 24, and a pre-rectifying tower second pressure regulating valve 241 and a pre-rectifying tower forward-to-flare stop valve 242 are respectively arranged on the pre-rectifying tower forward-to-flare pipeline 24.
The prefractionation column pressure controller 16 is connected to the piping between the prefractionation column 13 and the prefractionation column condenser 15 for monitoring and regulating the pressure in the prefractionation system, and the prefractionation column pressure control line 22 is split into two branches connected to the prefractionation column low pressure nitrogen line 23 and the prefractionation column go-to flare line 24, respectively, and is located on the prefractionation column first pressure regulating valve 231 and the prefractionation column second pressure regulating valve 241. The prefractionation tower pressure controller 16 is used for monitoring and controlling the pressure in the prefractionation system, and adjusting the prefractionation tower first pressure regulating valve 231 and the prefractionation tower second pressure regulating valve 241 according to the pressure in the system, so as to realize the constant pressure in the prefractionation system.
The pre-rectifying tower reflux pump 19 is positioned on a pipeline below the pre-rectifying tower reflux tank 18, the product pipeline 25 for removing light components is connected to the bottom of the pre-rectifying tower 13, the pre-rectifying tower kettle pump 20 is arranged on the product pipeline 25 for removing light components, and is used for conveying products in the product pipeline 25 for removing light components to a rectifying system, wherein the product pipeline 25 for removing light components is connected with the rectifying tower 26 and is positioned in a position on the upper middle part of the rectifying tower 26.
The rectification system comprises a rectification column 26, a rectification column bottom reboiler 27, a rectification column condenser 28, a rectification column pressure controller 29, a rectification column vacuum system 30, a rectification column reflux drum 31, a rectification column reflux pump 32 and a rectification column bottom pump 33.
The rectifying tower condenser 28 is connected with the rectifying tower vacuum system 30 through a rectifying tower vacuum pipeline 34, a rectifying tower vacuum pipeline stop valve 341 is arranged on the rectifying tower vacuum pipeline 34, two branches are communicated with the rectifying tower vacuum pipeline 34, a rectifying tower low-pressure nitrogen pipeline 36 and a rectifying tower forward flare pipeline 37 are respectively arranged on the rectifying tower low-pressure nitrogen pipeline 36, a rectifying tower first pressure regulating valve 361 and a rectifying tower low-pressure nitrogen stop valve 362 are respectively arranged on the rectifying tower low-pressure nitrogen pipeline 36, and a rectifying tower second pressure regulating valve 371 and a rectifying tower forward flare stop valve 372 are respectively arranged on the rectifying tower forward flare pipeline 37.
The rectifying column pressure controller 29 is connected to a pipeline between the rectifying column 26 and the rectifying column condenser 28 for monitoring and controlling the pressure in the rectifying system, and the rectifying column pressure control pipeline 35 is divided into two branches at the end thereof, connected to the rectifying column low pressure nitrogen pipeline 36 and the rectifying column forward flare pipeline 37, respectively, and located on the rectifying column first pressure regulating valve 361 and the rectifying column second pressure regulating valve 371. The rectifying tower pressure controller 29 is used for monitoring and controlling the pressure in the rectifying system, and adjusting the first rectifying tower pressure regulating valve 361 and the second rectifying tower pressure regulating valve 371 according to the pressure in the system, so as to realize the constant pressure in the rectifying system.
The rectifying column reflux pump 32 is located on a pipeline below the rectifying column reflux drum 31, and the end of the product pipeline 39 is divided into two branches, which are respectively connected with the top of the rectifying column 26 and the rectifying column reflux pump 32.
The tower bottom heavy component pipeline 38 is connected to the bottom of the rectifying tower 26, and the rectifying tower bottom pump 33 is arranged on the tower bottom heavy component pipeline 38 and is used for outputting the tower bottom heavy component substances in the tower bottom heavy component pipeline 38.
The apparatus for conversion of octanol and butanol as described above, the process for conversion of octanol to butanol comprising:
(1) Closing an octenal shutoff valve 91 arranged on the octenal feeding pipeline 9;
(2) Completely evaporating octenal in the hydrogenation evaporator 2, discharging residual liquid phase substances into a waste liquid fuel tank by a bottom pump of the hydrogenation evaporator 2, condensing crude octanol into a hydrogenation gas-liquid separator 8, and completely discharging the crude octanol into a rectification system under the action of pressure;
(3) The pre-rectifying system and the rectifying system continue to operate, and the bottoms of the pre-rectifying tower 13 and the rectifying tower 26 are reduced to low liquid level on the premise of ensuring the quality of octanol products;
(4) Purging the hydrogenation system, the pre-rectification system and the materials in the rectification system to an intermediate tank area by using nitrogen, and comprehensively replacing the materials in the device until octanol does not exist in the system;
(5) Closing the pre-rectifying column vacuum pipeline stop valve 211 on the pre-rectifying column vacuum pipeline 21, and opening the pre-rectifying column low-pressure nitrogen stop valve 232 on the pre-rectifying column low-pressure nitrogen pipeline 23 and the pre-rectifying column to flare stop valve 242 on the pre-rectifying column to flare pipeline 24;
(6) Closing a rectifying column vacuum pipeline stop valve 341 on the rectifying column vacuum pipeline 34, and opening a rectifying column low-pressure nitrogen stop valve 362 on the rectifying column low-pressure nitrogen pipeline 36 and a rectifying column-to-flare stop valve 372 on the rectifying column-to-flare pipeline 37;
(7) The pressure in the pre-rectification and rectification system is monitored and regulated in real time through the rectification column pressure controller 16 and the rectification column pressure controller 29, the pressure is low, low-pressure nitrogen is added into the system through regulating the pre-rectification column first pressure regulating valve 231 and the rectification column first pressure regulating valve 361, and when the pressure is high, non-condensable gas in the system is sent to a torch through regulating the pre-rectification column second pressure regulating valve 241 and the rectification column second pressure regulating valve 371, so that the constant micro-positive pressure state in the pre-rectification and rectification system is realized;
(8) The n-butyraldehyde stop valve 101 provided in the n-butyraldehyde feed line 10 is opened, and butanol production is started.
The apparatus for conversion of octanol and butanol as described above, the process for converting butanol to octanol is as follows:
(1) Closing a n-butyraldehyde stop valve 101 arranged on the n-butyraldehyde feeding pipeline 10;
(2) Completely evaporating butyraldehyde in the hydrogenation evaporator 2, discharging residual liquid phase substances into a waste liquid fuel tank by a bottom pump of the hydrogenation evaporator 2, condensing crude butanol to a hydrogenation gas-liquid separator 8, and completely discharging the crude butanol into a rectification system under the action of pressure;
(3) The pre-rectifying system and the rectifying system continue to operate, and the tower bottoms of the pre-rectifying tower 13 and the tower bottoms of the rectifying tower 26 are reduced to low liquid level on the premise of ensuring the quality of butanol products;
(4) Purging the hydrogenation system, the pre-rectification system and materials in the rectification system to an intermediate tank area by using nitrogen, and comprehensively replacing the materials in the device until no butanol exists in the system;
(5) Closing the pre-rectifying column low-pressure nitrogen stop valve 232 on the pre-rectifying column low-pressure nitrogen line 23 and the pre-rectifying column-to-flare stop valve 242 on the pre-rectifying column-to-flare line 24, and opening the pre-rectifying column vacuum line stop valve 211 on the pre-rectifying column vacuum line 21;
(6) Closing a rectifying column low-pressure nitrogen stop valve 362 on the rectifying column low-pressure nitrogen line 36 and a rectifying column-to-flare stop valve 372 on the rectifying column-to-flare line 37, and opening a rectifying column vacuum line stop valve 341 on the rectifying column vacuum line 34;
(7) The vacuum system 17 and the vacuum system 30 are utilized to respectively vacuumize the pre-rectification system and the rectification system, and the pressure in the pre-rectification system and the rectification system is monitored and regulated in real time through the rectification tower pressure controller 16 and the rectification tower pressure controller 29, so that the constant vacuum state in the pre-rectification system and the rectification system is ensured.
(8) The octenal shutoff valve 91 on the octenal feed line 9 was opened to start production of octanol.
In the embodiment, the butyraldehyde feeding pipeline from the tank area is added on the octenal feeding pipeline of the hydrogenation evaporator, and the n-butyraldehyde can enter the hydrogenation system from the pipeline, so that the hydrogenation system can be used for hydrogenating octenal and also can be used for hydrogenating butyraldehyde, the applicability of the hydrogenation system is improved, and the equipment investment is saved.
In the embodiment, a low-pressure nitrogen pipeline of the pre-rectifying tower and a pipeline of the pre-rectifying tower which is connected to a torch are added to a vacuum pipeline of the pre-rectifying tower in the pre-rectifying system, so that the pre-rectifying system can be used for pre-rectifying crude octanol and pre-rectifying crude butanol, the applicability of the pre-rectifying system is improved, and the equipment investment is saved.
In the embodiment, the rectification system is added with a low-pressure nitrogen pipeline of the rectification tower and a pipeline of the rectification tower which is connected with a torch, so that the rectification system can be used for rectifying octanol products for removing light components and butanol products for removing light components, the applicability of the rectification system is improved, and the equipment investment is saved.
In this embodiment, under the prerequisite that the device did not change, carry out a series of simple operations and valve control, can be according to octanol and butanol's market demand, realize octanol apparatus for producing and butanol apparatus for producing's mutual switch, increased the suitability of whole device, reduced the device cost of chemical plant, reduced area.
While the foregoing has been described in terms of illustrative embodiments of the invention, so that those skilled in the art may appreciate the invention, it is not to be restricted to the specific embodiments thereof, but only by the spirit and scope of the invention as defined and determined by the appended claims.
Claims (2)
1. The utility model provides a device suitable for octanol and butanol conversion production, includes condensation system (1), hydrogenation, pre-rectification system and rectification system, and hydrogenation includes hydrogenation evaporator (2), hydrogenation reactor (4), and pre-rectification system includes pre-rectification tower (13), pre-rectification tower condenser (15) and pre-rectification tower vacuum system (17), and rectification system includes rectifying column (26), rectifying column condenser (28) and rectifying column vacuum system (30), its characterized in that: an octenal feeding pipeline (9) is arranged between the condensation system (1) and the hydrogenation evaporator (2), a n-butyraldehyde feeding pipeline (10) is communicated with the octenal feeding pipeline (9), a pre-rectifying tower condenser (15) is connected with a pre-rectifying tower vacuum system (17) through a pre-rectifying tower vacuum pipeline (21), a pre-rectifying tower low-pressure nitrogen pipeline (23) and a pre-rectifying tower forward flare pipeline (24) are communicated with the pre-rectifying tower vacuum pipeline (21), a rectifying tower condenser (28) is connected with the rectifying tower vacuum system (30) through a rectifying tower vacuum pipeline (34), and a rectifying tower low-pressure nitrogen pipeline (36) and a rectifying tower forward flare pipeline (37) are communicated with the rectifying tower vacuum pipeline (34).
The hydrogenation system further comprises a hydrogenation feeding heater (3), a hydrogenation circulating compressor (5), a hydrogenation heat exchanger (6), a hydrogenation condenser (7) and a hydrogenation gas-liquid separator (8), wherein a crude hydrogenation product pipeline (12) is arranged at the lower end of the hydrogenation gas-liquid separator (8);
the pre-rectifying system further comprises a pre-rectifying tower bottom reboiler (14), a pre-rectifying tower pressure controller (16), a pre-rectifying tower reflux tank (18), a pre-rectifying tower reflux pump (19) and a pre-rectifying tower kettle pump (20), wherein a pre-rectifying tower pressure control pipeline (22) is respectively connected with the pre-rectifying tower low-pressure nitrogen pipeline (23) and the pre-rectifying tower forward-to-flare pipeline (24), and a light component removal product pipeline (25) is connected to the bottom of the pre-rectifying tower (13);
the rectifying system further comprises a rectifying tower bottom reboiler (27), a rectifying tower pressure controller (29), a rectifying tower reflux tank (31), a rectifying tower reflux pump (32) and a rectifying tower kettle pump (33), wherein a rectifying tower pressure control pipeline (35) is respectively connected with the rectifying tower low-pressure nitrogen pipeline (36) and the rectifying tower forward flare pipeline (37), a product pipeline (39) is connected with the rectifying tower reflux pump (32), and a tower kettle heavy component pipeline (38) is connected to the bottom of the rectifying tower (26);
a method for converting production of octanol to production of butanol, comprising:
(1) Stopping octenal feed;
(2) Completely evaporating octenal in the hydrogenation evaporator (2), and completely discharging the crude octanol into a rectification system under the action of pressure;
(3) The pre-rectifying system and the rectifying system continue to operate, and the tower bottoms of the pre-rectifying tower (13) and the rectifying tower (26) are reduced to low liquid level;
(4) Purging the hydrogenation system, the pre-rectification system and the materials in the rectification system to an intermediate tank area by using nitrogen, and comprehensively replacing the materials in the device until octanol does not exist in the system;
(5) Cutting off a vacuum pipeline (21) of the pre-rectifying tower, and opening a low-pressure nitrogen pipeline (23) of the pre-rectifying tower and a flare pipeline (24) of the pre-rectifying tower;
(6) Cutting off a vacuum pipeline (34) of the rectifying tower, and opening a low-pressure nitrogen pipeline (36) of the rectifying tower and a flare pipeline (37) of the rectifying tower;
(7) Regulating the internal of the pre-rectification and rectification system to be in a constant micro-positive pressure state;
(8) The n-butyraldehyde feed was started.
2. A method for converting butanol to octanol production based on the apparatus of claim 1 adapted for octanol and butanol conversion production, wherein:
(1) Stopping feeding the n-butyraldehyde;
(2) Completely evaporating butyraldehyde in the hydrogenation evaporator (2), and completely discharging crude butanol into a rectification system under the action of pressure;
(3) The pre-rectifying system and the rectifying system continue to operate, and the tower bottoms of the pre-rectifying tower (13) and the rectifying tower (26) are reduced to low liquid level;
(4) Purging the hydrogenation system, the pre-rectification system and materials in the rectification system to an intermediate tank area by using nitrogen, and comprehensively replacing the materials in the device until no butanol exists in the system;
(5) Cutting off a low-pressure nitrogen pipeline (23) of the pre-rectifying tower and a flare pipeline (24) of the pre-rectifying tower, and opening a vacuum pipeline (21) of the pre-rectifying tower;
(6) Cutting off a low-pressure nitrogen pipeline (36) of the rectifying tower and a flare pipeline (37) of the rectifying tower, and opening a vacuum pipeline (34) of the rectifying tower;
(7) Vacuumizing the pre-rectification and rectification system;
(8) The octenal feed was started.
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