CN115106025B - Environment-friendly and energy-saving dimethylformamide production device and production method - Google Patents
Environment-friendly and energy-saving dimethylformamide production device and production method Download PDFInfo
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C—CHEMISTRY; METALLURGY
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- C07C231/00—Preparation of carboxylic acid amides
- C07C231/22—Separation; Purification; Stabilisation; Use of additives
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- B01J2208/00106—Controlling the temperature by indirect heat exchange
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Abstract
The invention belongs to the technical field of dimethylformamide production, and discloses an environment-friendly and energy-saving dimethylformamide production device which comprises a tail gas condenser, a synthesis reactor, a first separator, a reaction cooler, a second separator, a dimethylamine cooler and a dimethylamine circulating pump. According to the invention, two separators and two condensers are additionally arranged to replace a circulating liquid cooler and a soft water cooler in the original process flow, and dimethylamine is changed into indirect feeding to replace the direct feeding of dimethylamine into a synthesis reactor in the original process flow, so that the dimethylamine containing trace water is prevented from directly entering the synthesis reactor and reacting with sodium methoxide catalyst to generate catalyst slag substances, the substances are prevented from being separated out on the pipe walls of the reaction cooler and the dimethylamine cooler, the problem that the heat exchange pipe of the cooler is blocked by the catalyst slag substances in the production process is thoroughly solved, and the production process is more environment-friendly, energy-saving and safer.
Description
Technical Field
The invention belongs to the technical field of dimethylformamide production, and relates to an environment-friendly and energy-saving dimethylformamide production device and method.
Background
Dimethylformamide (DMF) is an important organic chemical raw material and an excellent aprotic polar organic solvent. It can be mixed with water, diethyl ether, ethanol, kerosene, chlorinated hydrocarbon, aromatic hydrocarbon and most organic solvents, and can dissolve polymers such as ethyl cellulose, nitrocellulose, butyl acetate cellulose, polyacrylonitrile, vinyl chloride and polyvinyl chloride at normal temperature, and is called as a totipotent solvent; DMF is used as raw material, and can be used for synthesizing amine, amide, ether, aldehyde, nitrile, peptide, halogenated, heterocycle and phosphorus-containing compound, and can also be used for producing medicines such as cortisone, chlorphenamine, doxycycline, vitamin B6, and flex-expelling agent; can be used as a catalyst for chemical reaction; DMF can be used as a solvent for wet polyurethane synthetic leather and a solvent for preparing acrylic fibers and synthetic fibers by dry spinning of polyacrylonitrile; DMF may be used as an extractant for separation of substances, such as for extraction of butadiene from ethylene cracking gas C4, etc.
The main production process of DMF (shown in figure 1) is that dimethylamine and carbon monoxide react under the catalysis of sodium methoxide catalyst, and because dimethylamine as raw material used in the production process contains trace water, carbon monoxide contains trace carbon dioxide, oxygen, moisture and the like, the substances can react with sodium methoxide to produce sodium hydroxide, sodium carbonate, sodium formate and the like, the solubility of the substances in DMF solution is very small, and the substances are easy to separate out on the pipe wall of a heat exchange pipe of a DMF water cooler. These substances are continuously separated out on the heat exchange tube, so that the heat exchange efficiency of the heat exchanger is affected, the flow area of the heat exchange tube is blocked, the heat exchange capacity of the heat exchanger is continuously reduced, and finally, the heat released during DMF synthesis cannot be timely taken away, so that the synthesis reactor is overtemperature, the water cooler is forced to be switched, the reaction materials in the water cooler are discharged, and the water cooler is cleaned by hot water, so that the heat exchange capacity of the water cooler is recovered. The water cooler can generate peculiar smell during cleaning, which affects the health of workers. The water cooler is cleaned by using high-temperature steam condensate, and accidents such as scalding and the like can occur due to improper operation. Each team cleans the water cooler, which increases the labor intensity of workers.
The materials in the water cooler are recovered before cleaning, but because of the more pipeline valves, the materials in the system are difficult to clean, a large amount of organic wastewater is generated when the water cooler is cleaned by hot water, and the wastewater contains a large amount of amide substances, so that the wastewater has a bactericidal effect and cannot be directly subjected to biochemical treatment. The treatment methods commonly used at present are as follows: the incinerator is used for incineration treatment, but the waste water contains a large amount of sodium salt, so that the sodium salt severely corrodes the incinerator wall; if sodium hydroxide is adopted for alkaline hydrolysis, DMF and sodium hydroxide react to produce dimethylamine and sodium formate, so that a large amount of steam and sodium hydroxide are consumed, and large sodium salt wastewater is produced, and the operation cost is high.
Thus, there is a need for improved processes for the production of dimethylformamide.
Disclosure of Invention
The invention aims to provide an environment-friendly and energy-saving dimethylformamide production device and a production method, which thoroughly solve the problem that a cooler heat exchange tube is blocked by catalyst slag substances in the production process, solve the problem that a cooler needs frequent switching and cleaning to generate a large amount of high-content amide organic wastewater, improve the heat exchange effect of the cooler, reduce the occurrence of scalding accidents, lighten the labor intensity of operators, and are more environment-friendly, energy-saving and safer.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
the invention provides an environment-friendly and energy-saving dimethylformamide production device, which comprises a tail gas condenser, a synthesis reactor, a first separator, a reaction cooler, a second separator, a dimethylamine cooler and a dimethylamine circulating pump, wherein the tail gas condenser is connected with the reaction cooler; the method comprises the steps that a CO inlet and a catalyst inlet of a synthesis reactor are respectively connected with a CO conveying pipeline and a catalyst conveying pipeline, a gas outlet at the top of the synthesis reactor is sequentially connected with a gas inlet of a condenser and a gas inlet of a tail gas condenser through pipelines, a condensate outlet of the condenser and a condensate outlet of the tail gas condenser are connected with a condensate inlet at the lower part of the synthesis reactor through pipelines, a DMF outlet at the bottom of the synthesis reactor is connected with a liquid inlet at the upper part of a first separator through pipelines, a gas outlet at the top of the first separator is connected with a gas inlet of a reaction cooler through pipelines, a condensate outlet of the reaction cooler is connected with a condensate inlet of a second separator through pipelines, a DMF outlet at the bottom of the first separator is respectively connected with a circulating liquid inlet at the lower part of the second separator and a subsequent rectifying system through pipelines, a dimethylamine outlet at the top of the second separator is connected with a dimethylamine inlet of the synthesis reactor through pipelines, a dimethylamine inlet at the middle part of the second separator is connected with a dimethylamine conveying pipeline, and a condensate outlet of the dimethylamine cooler is connected with a condensate inlet of the second separator through pipelines.
In one technical scheme, the noncondensable gas outlet of the tail gas condenser is connected with a torch system through a pipeline.
In one technical scheme, the non-condensable gas outlet of the reaction cooler and the non-condensable gas outlet of the dimethylamine cooler are both connected with a flare system through pipelines.
In one technical scheme, a serpentine coil is arranged in the synthesis reactor, and one end of the serpentine coil is connected with a steam pipeline, and the other end of the serpentine coil is connected with a condensate pipeline.
In one technical scheme, be provided with the CO distributor in the synthetic reactor, the CO distributor comprises the inside and outside multilayer gas distribution pipe of annular distribution, and outer gas distribution pipe communicates each other with the inlayer gas distribution pipe through two distributing branch pipes of alternately distributing, sets up a plurality of shower nozzles along the circumference on the inlayer gas distribution pipe.
In a preferred technical scheme, the pipe diameter of the outer-layer gas distribution pipe is larger than that of the inner-layer gas distribution pipe.
The invention also provides an environment-friendly and energy-saving dimethylformamide production method, which comprises the following steps of:
2.3MPa of catalyst enters the upper part of the synthesis reactor through a catalyst inlet, and 2.3MPa of CO enters the lower part of the synthesis reactor through a CO inlet;
dimethylamine enters the second separator through a dimethylamine inlet, the dimethylamine is utilized to absorb heat by vaporization to reduce the temperature of a synthetic material, the vaporized dimethylamine steam is cooled by a dimethylamine cooler and then condensed into liquid dimethylamine, the liquid dimethylamine returns to the second separator by gravity for recycling, the dimethylamine is continuously vaporized and condensed to indirectly finish cooling the circulating liquid entering the second separator, the circulating liquid containing dimethylamine, which is discharged from the bottom of the second separator, enters the upper part of the synthesis reactor through the dimethylamine inlet after being pressurized by a pump to take away the heat released by the synthesis reaction, and the operation temperature of the synthesis reactor is 110-120 ℃ and the operation pressure is 2.0MPa;
unreacted gas phase materials in the synthesis reactor enter a condenser from the top, condensate returns to the synthesis reactor through a condensate inlet after being cooled, noncondensable gas enters a tail gas condenser, condensate returns to the synthesis reactor through a condensate inlet after being condensed, and top noncondensable gas is sent to a flare system;
and (3) enabling DMF at the bottom of the synthesis reactor to enter a first separator, enabling gas at the top of the first separator to enter a reaction cooler for cooling after flash evaporation, enabling condensate to enter a second separator, enabling non-condensable gas to be sent to a torch for incineration, enabling a part of DMF at the bottom of the first separator to be sent to a subsequent rectifying system, and enabling a part of DMF at the bottom of the first separator to be sent into the second separator as circulating liquid to be mixed with dimethylamine.
In one technical scheme, the operating pressure of the first separator is 0.6-0.7 MPa, and the operating pressure of the second separator is 0.55-0.65 MPa.
In one technical scheme, a serpentine coil is arranged in the synthesis reactor, one end of the serpentine coil is connected with a steam pipeline, the other end of the serpentine coil is connected with a condensate pipeline, steam is used for heating circulating liquid in the synthesis reactor by starting the serpentine coil in the start-up stage of the synthesis reactor, and when the temperature in the synthesis reactor reaches more than 85 ℃, CO is introduced into the synthesis reactor, and dimethylamine is added into the second separator.
In one technical scheme, a CO distributor is arranged in the synthesis reactor and is used for uniformly distributing CO introduced into the synthesis reactor.
Compared with the prior art, the invention has the beneficial effects that:
the invention adds two separators and two condensers to replace the circulating liquid cooler and soft water cooler in the original process flow, simultaneously, the circulating liquid entering the second separator is cooled indirectly by continuously gasifying and condensing dimethylamine in the second separator and the dimethylamine cooler, and then the circulating liquid containing dimethylamine from the bottom of the second separator enters the upper part of the synthesis reactor through a dimethylamine inlet after being pressurized by a pump to take away the heat released by the synthesis reaction, thereby replacing the prior process flow to directly enter dimethylamine into the synthesis reactor, thereby avoiding the dimethylamine containing trace water from directly entering the synthesis reactor to react with sodium methoxide catalyst to generate catalyst slag substances with lower solubility in DMF solution, such as sodium hydroxide, sodium carbonate, sodium formate and the like, and avoiding the precipitation of the substances on the pipe wall of the reaction cooler, and the invention comprises the following steps: 1) Thoroughly solves the problem that the heat exchange tube of the cooler is blocked by catalyst slag substances in the production process, and ensures the stability and continuity of DMF production; 2) Solves the problem that the cooler is blocked and needs frequent switching and cleaning to generate a large amount of high-content amide organic wastewater, so the production method is more environment-friendly; 3) Because the cooler has no blockage problem, the heat exchange effect of the cooler is improved, the circulation volume of the circulating liquid entering the synthesis reactor is greatly reduced, the power of the circulating pump is reduced by more than 50 percent, and meanwhile, a soft water circulating pump is omitted, so that the production method is more energy-saving; 4) The method reduces the steps of using hot water to clean the catalyst residues on the cooler, reduces the occurrence of scalding accidents, and also reduces the labor intensity of operators, so that the production method is safer.
Drawings
FIG. 1 is a flow chart of a prior art dimethylformamide production process.
FIG. 2 is a flow chart of the dimethylformamide production process according to the present invention.
FIG. 3 is a schematic diagram of the structure of a serpentine coil in a synthesis reactor according to the present invention.
FIG. 4 is a schematic diagram of the structure of a CO distributor in the synthesis reactor of the present invention.
The reference numbers in the drawings: the device comprises a tail gas condenser 1, a condenser 2, a synthesis reactor 3, a synthesis circulating pump 4, a circulating liquid cooler 5, a soft water circulating pump 6, a soft water cooler 7, a first separator 8, a reaction cooler 9, a second separator 10, a dimethylamine cooler 11, a dimethylamine pump 12, a serpentine coil 13 and a CO distributor 14.
Detailed Description
The following examples are illustrative of the present invention and are not intended to limit the scope of the invention. The technical means used in the examples are conventional means well known to those skilled in the art unless otherwise indicated. The test methods in the following examples are conventional methods unless otherwise specified.
Example 1
As shown in fig. 2, the invention relates to an environment-friendly and energy-saving dimethylformamide production device, which comprises a tail gas condenser 1, a condenser 2, a synthesis reactor 3, a first separator 8, a reaction cooler 9, a second separator 10, a dimethylamine cooler 11 and a dimethylamine circulating pump 12.
The connection relation of each device in the production device is determined according to the material trend, and the connection relation is specifically as follows: the CO inlet and the catalyst inlet of the synthesis reactor 3 are respectively connected with a CO material conveying pipeline and a catalyst material conveying pipeline, the gas outlet at the top of the synthesis reactor 3 is sequentially connected with the gas inlet of the condenser 2 and the gas inlet of the tail gas condenser 1 through pipelines, the condensate outlet of the condenser 2 and the condensate outlet of the tail gas condenser 1 are connected with the gas inlet at the lower part of the synthesis reactor 3 through pipelines, the DMF outlet at the bottom of the synthesis reactor 3 is connected with the liquid inlet at the upper part of the first separator 8 through pipelines, the gas outlet at the top of the first separator 8 is connected with the gas inlet of the reaction cooler 9 through pipelines, the condensate outlet of the reaction cooler 9 is connected with the condensate inlet of the second separator (10) through pipelines, the DMF outlet at the bottom of the first separator 8 is respectively connected with the circulating liquid inlet at the lower part of the second separator 10 and the subsequent rectification system through pipelines, the gas outlet at the top of the second separator 10 is connected with the gas inlet of the dimethylamine cooler 11 through pipelines, the dimethylamine outlet at the bottom of the second separator 10 is connected with the dimethylamine inlet of the synthesis reactor 3 through pipelines, the dimethylamine inlet at the middle part of the second separator 10 is connected with the dimethylamine inlet of the dimethylamine cooler through pipelines, and the condensate outlet of the dimethylamine cooler 11 is connected with the condensate inlet of the second separator 10.
As shown in fig. 2, the condenser 2, the reaction cooler 9 and the dimethylamine cooler 11 in the invention are all cooled by circulating water, the tail gas condenser 1 is cooled by a methanol water solution with the temperature of minus 10 ℃, and the non-condensable gas outlet of the tail gas condenser 1, the non-condensable gas outlet of the reaction cooler 9 and the non-condensable gas outlet of the dimethylamine cooler 11 are all connected with a torch system through pipelines.
As shown in figure 3, in order to meet the heating requirement of the synthesis reactor 3 in the starting stage, a group of serpentine coils 13 are arranged in the synthesis reactor 3, one end of each serpentine coil 13 is connected with a steam pipeline, the other end is connected with a condensate pipeline, circulating liquid is directly heated by steam to heat, when the temperature in the synthesis reactor 3 reaches more than 85 ℃, CO is introduced into the synthesis reactor 3, dimethylamine is added into the second separator 10, the components of the reaction liquid are analyzed, the catalyst addition amount is determined according to the water content, the reactor pressure is controlled to be less than or equal to 2.0MPa (G), the temperature is controlled to be between 110 and 120 ℃, and the liquid level is controlled to be about 80%.
As shown in fig. 4, a CO distributor 14 is provided in the synthesis reactor 3 to uniformly distribute CO introduced into the synthesis reactor 3. The CO distributor 14 is composed of an inner layer gas distribution pipe and an outer layer gas distribution pipe which are distributed in a ring shape, and the outer layer gas distribution pipe is communicated with the inner layer gas distribution pipe through two distribution branch pipes which are distributed in a cross mode, a plurality of spray heads are evenly arranged on the inner layer gas distribution pipe along the circumference, and the pipe diameter of the outer layer gas distribution pipe is larger than that of the inner layer gas distribution pipe.
It should be noted that the serpentine coil 13 and the CO distributor 14 disposed in the synthesis reactor 3 according to the present invention have upper and lower positions, and in order to prevent the serpentine coil 13 from affecting the gas distribution effect of CO in the synthesis reactor 3, the CO distributor 14 is disposed above the serpentine coil 13.
The production method of the dimethylformamide based on the production device comprises the following steps:
2.3MPa sodium methoxide catalyst enters the upper part of the synthesis reactor 3 through a catalyst inlet, and 2.3MPa CO from the gasification device enters the lower part of the synthesis reactor 3 through a CO inlet;
dimethylamine from a methylamine device enters the second separator 10 through a dimethylamine inlet, the dimethylamine is utilized to absorb heat by vaporization to reduce the temperature of a synthetic material, vaporized dimethylamine steam is cooled by a dimethylamine cooler 11 and then condensed into liquid dimethylamine, the liquid dimethylamine returns to the second separator 10 by gravity for recycling, the dimethylamine is continuously vaporized and condensed to indirectly finish cooling the circulating liquid entering the second separator 10, the circulating liquid containing dimethylamine from the bottom of the second separator 10 is pressurized by a dimethylamine pump 12 and then enters the upper part of the synthesis reactor 3 through the dimethylamine inlet to take away the heat released by the synthesis reaction, the operating temperature of the synthesis reactor 3 is 110-120 ℃, and the operating pressure is 2.0MPa;
unreacted gas phase materials in the synthesis reactor 3 enter the condenser 2 from the top, condensate is cooled and then returned to the synthesis reactor 3 through a condensate inlet, noncondensable gas enters the tail gas condenser 1, condensate is condensed and then returned to the synthesis reactor 3 through a condensate inlet, and the top noncondensable gas is sent to a torch system;
DMF at the bottom of the synthesis reactor 3 enters a first separator 8, gas at the top of the first separator 8 enters a reaction cooler 9 for cooling after flash evaporation, condensate enters a second separator 10, noncondensable gas is sent to a torch for incineration, and a part of DMF at the bottom of the first separator 8 is sent to a subsequent rectifying system, and the other part of DMF is sent into the second separator 10 as circulating liquid to be mixed with dimethylamine.
In one embodiment, the operation pressure of the first separator 8 is 0.6-0.7 mpa, and the operation pressure of the second separator is 0.55-0.65 mpa, so that a better gas-liquid separation effect can be achieved.
In the dimethylformamide production process, two separators (a first separator 8 and a second separator 10) and two condensers (a reaction cooler 9 and a dimethylamine cooler 11) are additionally arranged to replace a circulating liquid cooler 5 and a soft water cooler 7 in the original process flow, and simultaneously, the circulating liquid entering the second separator 10 is cooled indirectly by continuously gasifying and condensing dimethylamine in the second separator 10 and the dimethylamine cooler 11, and then the circulating liquid containing dimethylamine, which is discharged from the bottom of the second separator 10, enters the upper part of the synthesis reactor 3 through a dimethylamine inlet after being pressurized by a pump so as to take away the heat released by the synthesis reaction, and replaces the prior process flow to directly enter the dimethylamine into the synthesis reactor, thereby avoiding the direct entering of the dimethylamine containing trace water into the synthesis reactor 3, reacting with sodium methoxide catalyst to generate catalyst slag substances with lower solubility in DMF solution, such as sodium carbonate, sodium formate and the like, and avoiding the precipitation of the substances on the pipe wall of the reaction cooler 9, so that: 1) Thoroughly solves the problem that the heat exchange tube of the cooler is blocked by catalyst slag substances in the production process, and ensures the stability and continuity of DMF production; 2) Solves the problem that the cooler is blocked and needs frequent switching and cleaning to generate a large amount of high-content amide organic wastewater, so the production method is more environment-friendly; 3) Because the cooler has no blockage problem, the heat exchange effect of the cooler is improved, the circulation volume of the circulating liquid entering the synthesis reactor is greatly reduced, the power of the circulating pump is reduced by more than 50 percent, and meanwhile, the soft water circulating pump 6 (the power of the synthesis circulating pump is equivalent to that of the dimethylamine pump 12) is omitted, so that the production method is more energy-saving; 4) The method reduces the steps of using hot water to clean the catalyst residues on the cooler, reduces the occurrence of scalding accidents, and also reduces the labor intensity of operators, so that the production method is safer.
The above-mentioned embodiments are merely preferred embodiments of the present invention, which are not intended to limit the scope of the present invention, and other embodiments can be easily made by those skilled in the art through substitution or modification according to the technical disclosure in the present specification, so that all changes and modifications made in the principle of the present invention shall be included in the scope of the present invention.
Claims (10)
1. The production device of the dimethylformamide comprises a tail gas condenser (1), a condenser (2) and a synthesis reactor (3), and is characterized by further comprising a first separator (8), a reaction cooler (9), a second separator (10), a dimethylamine cooler (11) and a dimethylamine circulating pump (12); the CO inlet and the catalyst inlet of the synthesis reactor (3) are respectively connected with a CO material conveying pipeline and a catalyst material conveying pipeline, the gas outlet at the top of the synthesis reactor (3) is sequentially connected with the gas inlet of the condenser (2) and the gas inlet of the tail gas condenser (1) through pipelines, the condensate outlet of the condenser (2) and the condensate outlet of the tail gas condenser (1) are respectively connected with the condensate inlet at the lower part of the synthesis reactor (3) through pipelines, the DMF outlet at the bottom of the synthesis reactor (3) is connected with the liquid inlet at the upper part of the first separator (8) through pipelines, the gas outlet at the top of the first separator (8) is connected with the gas inlet of the reaction cooler (9) through pipelines, the condensate outlet of the reaction cooler (9) is connected with the condensate inlet of the second separator (10) through pipelines, the DMF outlet at the bottom of the first separator (8) is respectively connected with the circulating liquid inlet at the lower part of the second separator (10) and the subsequent rectification system through pipelines, the gas outlet at the top of the second separator (10) is connected with the gas inlet of the dimethylamine cooler (11) through pipelines, the dimethylamine outlet at the bottom of the second separator (10) is connected with the dimethylamine inlet at the middle part of the second separator (3) through pipelines, the condensate outlet of the dimethylamine cooler (11) is connected with the condensate inlet of the second separator (10) through a pipeline.
2. The production plant according to claim 1, characterized in that the noncondensable gas outlet of the off-gas condenser (1) is connected to a flare system by means of a pipe.
3. The production plant according to claim 1, characterized in that the non-condensable gas outlet of the reaction cooler (9) and the non-condensable gas outlet of the dimethylamine cooler (11) are both connected to a flare system by piping.
4. The production device according to claim 1, characterized in that a serpentine coil (13) is arranged in the synthesis reactor (3), one end of the serpentine coil (13) being connected to a steam pipe and the other end being connected to a condensate pipe.
5. The production device according to claim 1, wherein a CO distributor (14) is arranged in the synthesis reactor (3), the CO distributor (14) is composed of an inner layer gas distribution pipe and an outer layer gas distribution pipe which are distributed in a ring shape, the outer layer gas distribution pipe is mutually communicated with the inner layer gas distribution pipe through two distribution branch pipes which are distributed in a crossed manner, and a plurality of spray heads are arranged on the inner layer gas distribution pipe along the circumference.
6. The apparatus for producing of claim 5, wherein the pipe diameter of the outer cloth pipe is greater than the pipe diameter of the inner cloth pipe.
7. The method for producing dimethylformamide based on the production apparatus according to any one of claims 1 to 6, comprising the steps of:
2.3MPa of catalyst enters the upper part of the synthesis reactor (3) through a catalyst inlet, and 2.3MPa of CO enters the lower part of the synthesis reactor (3) through a CO inlet;
dimethylamine enters the second separator (10) through a dimethylamine inlet, the temperature of a synthetic material is reduced by utilizing dimethylamine vaporization and absorption heat, vaporized dimethylamine steam is cooled by a dimethylamine cooler (11) and then condensed into liquid dimethylamine, the liquid dimethylamine returns to the second separator (10) by gravity for recycling, the dimethylamine is continuously vaporized and condensed to indirectly finish cooling the circulating liquid entering the second separator (10), the circulating liquid containing dimethylamine, which is discharged from the bottom of the second separator (10), enters the upper part of the synthesis reactor (3) through the dimethylamine inlet after being pressurized by a pump so as to take away the heat released by the synthesis reaction, and the operating temperature of the synthesis reactor (3) is 110-120 ℃ and the operating pressure is 2.0MPa;
unreacted gas phase materials in the synthesis reactor (3) enter the condenser (2) from the top, condensate returns to the synthesis reactor (3) through a condensate inlet after being cooled, noncondensable gas enters the tail gas condenser (1), condensate returns to the synthesis reactor (3) through a condensate inlet after being condensed, and the top noncondensable gas is sent to a torch system;
DMF at the bottom of the synthesis reactor (3) enters a first separator (8), gas at the top of the first separator (8) enters a reaction cooler (9) for cooling after flash evaporation, condensate enters a second separator (10), non-condensable gas is sent to a torch for incineration, a part of DMF at the bottom of the first separator (8) is sent to a subsequent rectifying system, and the other part of DMF is sent into the second separator (10) as circulating liquid for mixing with dimethylamine.
8. The dimethylformamide production process according to claim 7, wherein the operating pressure of the first separator (8) is 0.6 to 0.7mpa and the operating pressure of the second separator is 0.55 to 0.65mpa.
9. The dimethylformamide production method as claimed in claim 7, wherein a serpentine coil (13) is arranged in the synthesis reactor (3), one end of the serpentine coil (13) is connected with a steam pipeline, the other end of the serpentine coil is connected with a condensate pipeline, the serpentine coil (13) is started to heat circulating liquid in the synthesis reactor (3) by utilizing steam in a starting stage of the synthesis reactor (3), and when the temperature in the synthesis reactor (3) reaches above 85 ℃, CO is introduced into the synthesis reactor (3), and dimethylamine is added into the second separator (10).
10. The dimethylformamide production process according to claim 7, wherein a CO distributor (14) is provided in the synthesis reactor (3) for uniformly distributing CO introduced into the synthesis reactor (3).
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