CN112745228A - Energy-saving separation process device and method for high-purity monomethylamine and dimethylamine - Google Patents
Energy-saving separation process device and method for high-purity monomethylamine and dimethylamine Download PDFInfo
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- CN112745228A CN112745228A CN202011617156.6A CN202011617156A CN112745228A CN 112745228 A CN112745228 A CN 112745228A CN 202011617156 A CN202011617156 A CN 202011617156A CN 112745228 A CN112745228 A CN 112745228A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/82—Purification; Separation; Stabilisation; Use of additives
- C07C209/86—Separation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/82—Purification; Separation; Stabilisation; Use of additives
- C07C209/84—Purification
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention relates to an energy-saving separation process method and a device of high-purity monomethylamine and dimethylamine. The invention adopts double-tower operation, the monomethylamine separation tower refines a high-purity monomethylamine product, the dimethylamine refining tower refines a high-purity dimethylamine product, and the operating pressure of the double towers is adjusted to ensure that the double towers form differential pressure so as to carry out heat integration, thereby improving the energy utilization efficiency, reducing the water consumption for cooling and lowering the process operation cost.
Description
Technical Field
The invention relates to the technical field of chemical separation, relates to a technology for separating monomethylamine and dimethylamine, and particularly relates to an energy-saving separation process device and method for high-purity monomethylamine and dimethylamine.
Background
In the existing four-tower methylamine production process, methanol, ammonia and circulating materials sequentially enter an ammonia still through a catalytic reactor to remove ammonia, tower bottom liquid enters an extraction tower to remove trimethylamine through water extraction, tower bottom liquid of the extraction tower enters a dehydration tower to be dehydrated, then mixed liquid of monomethylamine dimethylamine is obtained and enters a monomethylamine separation tower to be separated, monomethylamine is rectified and extracted from the top of the separation tower, and dimethylamine is extracted from a side line gas phase at the lower part of the separation tower. Dimethylamine extracted from the side line of the separation tower also contains impurities such as monomethylamine, water, methanol and the like, the monomethylamine product at the tower top contains the impurities such as dimethylamine and the like, and the impurities in the product influence the quality of downstream products.
The new national standard HG/T2972-2017 Industrial monomethylamine increases the requirement of anhydrous monomethylamine, and has low allowable content of impurities dimethylamine, trimethylamine and water. The requirement of anhydrous dimethylamine is increased in the new national standard of HG/T2973-2017 industrial dimethylamine, and the allowable impurity content is low. Liu Xiao Yu, Shen Ruan is put forward in the literature "methylamine device-methylamine product quality promotion summary", impurity dimethylamine in monomethylamine product can not reach the qualified product requirement in new national standard, reflux quantity of the separation tower is from 18m3The flow rate is increased to about 21-22 m3And h and other improvement measures, so that the quality index of the monomethylamine product produced at the top of the separation tower meets the new national standard requirement, the energy consumption is increased by about 17-22%, and the consumption of condensed water is increased. After the new national standard is implemented, in order to make the monomethylamine and dimethylamine products produced by the separation tower reach the standard, a large amount of energy consumption and condensed water are required to be increased.
In patent CN107311871B, the content of moisture and heavy components in dimethylamine is reduced by adding a side line tower, but the impurity dimethylamine in the monomethylamine product does not meet the requirement of qualified products in the new national standard, and the impurity monomethylamine in the dimethylamine only meets the requirement of first-class products in the new national standard. However, the quality of the monomethylamine and dimethylamine products separated by the main tower is not improved, the impurity dimethylamine in the monomethylamine products produced by the main tower is unqualified, the content of the impurity monomethylamine in the dimethylamine gas phase extracted from the side line of the main tower and entering the side line tower is higher, and the production is reduced under the condition that the energy consumption of the main tower is increased or is not changed if the monomethylamine and the dimethylamine products are qualified.
Disclosure of Invention
Aiming at the defects of the prior art, the invention discloses an energy-saving separation process device and method for high-purity monomethylamine dimethylamine, which are realized by respectively separating high-purity monomethylamine and dimethylamine products by double towers, and the operating pressure of the double towers is adjusted to enable the double towers to form differential pressure so as to carry out heat integration, save energy and reduce consumption.
The specific scheme of the invention is as follows:
an energy-saving separation method of high-purity monomethylamine dimethylamine comprises the steps of feeding monomethylamine dimethylamine mixed raw materials dehydrated by a dehydration tower from the middle part of a monomethylamine separation tower, rectifying a monomethylamine product from the top of the tower, sending the monomethylamine product to a monomethylamine product tank for storage, sending dimethylamine mixed liquor at the bottom of the tower to a dimethylamine separation tower, rectifying a dimethylamine product from the top of the tower, sending the dimethylamine product to a dimethylamine product tank, and discharging mixed liquor of recombinant water, methanol and the like at the bottom of the tower; wherein, the overhead gas of the dimethylamine knockout tower is used as the heat source of a reboiler of the monomethylamine knockout tower.
In the technical scheme, preferably, the operation pressure of the monomethylamine separation tower is 0.5-0.85 MPa absolute pressure, the number of theoretical plates is 50-100, the temperature at the top of the tower is 33-56 ℃, and the reflux ratio is 3.5-9.
In the technical scheme, preferably, the operating pressure of the dimethylamine separation tower is 0.7-1.4 MPa, the number of theoretical plates is 5-50, the temperature at the top of the tower is 60-98 ℃, the reflux ratio is 0.005-2, and the operating pressure of the dimethylamine separation tower is higher than that of the monomethylamine separation tower.
In the above technical solution, preferably, after heat exchange of overhead gas of the dimethylamine knockout tower as a heat source of the reboiler of the monomethylamine knockout tower, a part of overhead gas is refluxed to the dimethylamine knockout tower, and a part of overhead gas is extracted as a product.
In the above technical solution, preferably, the monomethylamine separation column and the dimethylamine separation column are any one or a combination of a plate column, a bulk packed column and a regular packed column.
The invention also provides an energy-saving separation process device of high-purity monomethylamine and dimethylamine, which comprises a monomethylamine separation tower and a dimethylamine separation tower, wherein the outlet at the top of the monomethylamine separation tower is sequentially connected with a monomethylamine separation tower condenser, a monomethylamine separation tower reflux tank and a monomethylamine separation tower reflux pump through an extraction pipeline; the first reboiler of a methylamine knockout tower is connected at the tower cauldron of methylamine knockout tower, the tower cauldron export of methylamine knockout tower is connected to the middle part feed inlet of dimethylamine knockout tower through adopting the pipeline, the top outlet of dimethylamine knockout tower connects gradually dimethylamine knockout tower condenser through adopting the pipeline, dimethylamine knockout tower reflux tank, dimethylamine knockout tower reflux pump, the outlet pipeline of dimethylamine knockout tower reflux pump divides into two routes, connect to the top reflux mouth of dimethylamine knockout tower on the same way, another way is connected to dimethylamine product jar through dimethylamine product condenser, connect dimethylamine knockout tower reboiler at the tower cauldron of dimethylamine knockout tower.
And the tower top outlet of the dimethylamine separation tower is connected with the shell pass inlet of the dimethylamine separation tower condenser, the shell pass outlet of the dimethylamine separation tower condenser is connected with a dimethylamine separation tower reflux tank, and the tube pass inlet and outlet of the dimethylamine separation tower condenser are respectively connected to a tower kettle of the monomethylamine separation tower and are used as a second reboiler of the monomethylamine separation tower.
The invention is also suitable for the reconstruction of the prior process device, adds a dimethylamine separation tower and constructs double-tower differential pressure heat integration with the original separation tower.
The energy-saving separation method of the high-purity monomethylamine dimethylamine has the beneficial effects that:
1. the invention adopts a methylamine separation tower and a dimethylamine separation tower to operate. The monomethylamine separation tower refines a high-purity monomethylamine product, so that the content of impurity dimethylamine in the monomethylamine product is lower than the requirement of a new national standard high-grade product, and meanwhile, the content of monomethylamine in tower bottom liquid is low, and even the content of impurity monomethylamine in the dimethylamine product after concentration by the dimethylamine separation tower is also lower than the requirement of the new national standard high-grade product, thereby avoiding unqualified content of impurity dimethylamine in the tower top monomethylamine product and unqualified content of impurity monomethylamine in a side-line dimethylamine product in the prior art. The dimethylamine refining tower refines a high-purity dimethylamine product, reduces the content of moisture and heavy components in the dimethylamine, and avoids discharging a large amount of dimethylamine product while discharging water from the tower kettle in the prior art.
2. The monomethylamine separation tower is not provided with a side line for dimethylamine gas phase extraction, so that the heat load of the monomethylamine separation tower is reduced. The operating pressure of the double towers is adjusted to enable the double towers to form differential pressure so as to carry out heat integration, all tower top gas of the dimethylamine separation tower is used as a heat source of a reboiler of the monomethylamine separation tower, the heat load of the monomethylamine separation tower is further reduced, the energy utilization efficiency is improved, the water consumption for cooling is reduced, and the process operation cost is reduced.
Drawings
FIG. 1 is a process flow diagram employed in the present invention.
In fig. 1, T101 is a monomethylamine separation tower, T102 is a dimethylamine separation tower, E101 is a first reboiler of the monomethylamine separation tower, E102 is a second reboiler of the monomethylamine separation tower and also serves as a condenser of the dimethylamine separation tower, E103 is a condenser of the monomethylamine separation tower, E201 is a reboiler of the dimethylamine separation tower, E202 is a condenser of the dimethylamine product, P101 is a reflux pump of the monomethylamine separation tower, P102 is a feed pump of the dimethylamine separation tower, P201 is a reflux pump of the dimethylamine separation tower, V101 is a reflux tank of the monomethylamine separation tower, V102 is a monomethylamine product tank, V201 is a reflux tank of the dimethylamine separation tower, V202 is a dimethylamine product tank, 1 is a monomethylamine and dimethylamine mixed raw material dehydrated by a dehydration tower, 2 is a dimethylamine mixed solution after removal of monomethylamine, 3 is a monomethylamine product liquid, 4 is an overhead gas of the dimethylamine separation tower, 5 is a dimethylamine product liquid, 6 is a, and a mixed liquid such as methanol.
Detailed Description
The energy-saving separation method of monomethylamine dimethylamine with high purity according to the present invention will be described in detail with reference to the following examples.
An energy-saving separation process device for high-purity monomethylamine and dimethylamine comprises a monomethylamine separation tower T101 and a dimethylamine separation tower T102, wherein a feed inlet is formed in the middle of the monomethylamine separation tower T101, the top outlet of the monomethylamine separation tower T101 is sequentially connected with a monomethylamine separation tower condenser E103, a monomethylamine separation tower reflux tank V101 and a monomethylamine separation tower reflux pump P101 through an extraction pipeline, the outlet pipeline of the monomethylamine separation tower reflux pump P101 is divided into two paths, one path is connected to the top reflux port of the monomethylamine separation tower T101, and the other path is connected to a monomethylamine product tank V102. A first reboiler E101 of a monomethylamine separation tower is connected to a tower kettle of the monomethylamine separation tower T101, a tower kettle outlet of the monomethylamine separation tower T101 is connected to a middle feed inlet of the dimethylamine separation tower T102 through an extraction pipeline, a dimethylamine separation tower feed pump P102 is installed on the extraction pipeline, a tower top outlet of the dimethylamine separation tower T102 is sequentially connected with a dimethylamine separation tower condenser E102, a dimethylamine separation tower reflux tank V201 and a dimethylamine separation tower reflux pump P201 through the extraction pipeline, an outlet pipeline of the dimethylamine separation tower reflux pump P201 is divided into two paths, one path is connected to a top reflux port of the dimethylamine separation tower T102, and the other path is connected to a dimethylamine product tank V202 through a dimethylamine product condenser E202. A reboiler E201 of the dimethylamine separator is connected to the bottom of the dimethylamine separator T102.
An outlet at the top of the dimethylamine separation tower T102 is connected with a shell-side inlet of the dimethylamine separation tower condenser E102, and a shell-side outlet of the dimethylamine separation tower condenser E102 is connected with a dimethylamine separation tower reflux tank V201. The tube pass inlet and outlet of the dimethylamine knockout tower condenser E102 are connected with a monomethylamine knockout tower T101 and used as a second reboiler of the monomethylamine knockout tower T101.
An energy-saving separation process method of high-purity monomethylamine and dimethylamine comprises the steps of feeding monomethylamine and dimethylamine mixed raw material 1 dehydrated by a dehydration tower from the middle part of a monomethylamine separation tower T101, supplying heat to the monomethylamine separation tower T101 by a first reboiler E101 of the monomethylamine separation tower, condensing tower overhead gas by a monomethylamine separation tower condenser E103, entering a monomethylamine separation tower reflux tank V101, pressurizing liquid in the reflux tank V101 by a monomethylamine separation tower reflux pump P101, refluxing a part of the liquid to the monomethylamine separation tower T101, sending a part of the liquid as monomethylamine product liquid 3 to a monomethylamine product tank V102 for storage, pressurizing dimethylamine mixed liquid 2 subjected to monomethylamine removal at a tower kettle by a dimethylamine separation tower feed pump P102, sending the dimethylamine mixed liquid to the dimethylamine separation tower T102, supplying heat to the dimethylamine separation tower reboiler E201, discharging mixed liquid 6 of recombinant water, methanol and the like from the tower kettle, condensing the dimethylamine separated tower overhead gas 4 after heat exchange by a second reboiler E102 of the methylamine separation tower and the dimethylamine separation tower condenser E And a methylamine separation tower reflux tank V201, wherein after the liquid in the reflux tank V201 is pressurized by a dimethylamine separation tower reflux pump P201, a part of the liquid reflows to the dimethylamine separation tower T102, and a part of the liquid is extracted as dimethylamine product liquid 5.
The operation pressure of the monomethylamine separation tower T101 is 0.5-0.85 MPa absolute pressure, the number of theoretical plates is 45-100, the temperature of the top of the tower is 33-56 ℃, and the reflux ratio is 3.5-9.
The operating pressure of the dimethylamine separation tower T102 is 0.7-1.4 MPa absolute pressure, the number of theoretical plates is 10-60, the temperature of the tower top is 60-98 ℃, the reflux ratio is 0.005-2, and the operating pressure of the dimethylamine separation tower T102 is higher than that of the monomethylamine separation tower T101.
The monomethylamine separation tower T101 and the dimethylamine separation tower T102 are any one or combination of a plate tower, a bulk packed tower or a regular packed tower.
Example 1
By adopting the flow chart shown in fig. 1, the monomethylamine dimethylamine mixed raw material is subjected to energy-saving separation, the feeding amount is 1000kg/h, the feeding temperature is 50 ℃, and the feeding composition is shown in the following table.
The operation pressure of the monomethylamine separation tower T101 is 0.62MPa absolute pressure, the number of theoretical plates is 52, the reflux ratio is 4.9, and the tower top temperature is 42 ℃.
The operating pressure of the dimethylamine separation tower T102 is 0.95MPa absolute pressure, the theoretical plate number is 30, the tower top temperature is 77.2 ℃, and the reflux ratio is 0.5. And (3) taking the overhead gas of the dimethylamine separation tower as a heat source of a reboiler of the monomethylamine separation tower.
The results of this process for the separation of the monomethylamine dimethylamine starting material are given in the following table.
The total heat load of the reboiler of the monomethylamine separation tower is 521kW, the heat load of the gas phase at the top of the dimethylamine separation tower is 99kW, and the heat load can be saved by 19% by using the overhead gas of the dimethylamine separation tower as the heat source of the reboiler of the monomethylamine separation tower. Namely, 422kW heat load needs to be supplemented to a reboiler of the monomethylamine separation tower, and the rest is provided by a gas phase at the top of the second tower.
By the process, the high-purity monomethylamine and dimethylamine products can be obtained by mixing the monomethylamine and dimethylamine raw materials.
Example 2
By adopting the flow chart shown in fig. 1, the monomethylamine dimethylamine mixed raw material is subjected to energy-saving separation, the feeding amount is 2000kg/h, the feeding temperature is 50 ℃, and the feeding composition is shown in the following table.
The operation pressure of the monomethylamine separation tower T101 is 0.58MPa absolute pressure, the theoretical plate number is 62, the reflux ratio is 4.6, and the tower top temperature is 40 ℃.
The operating pressure of the dimethylamine separation tower T102 is 0.9MPa absolute pressure, the theoretical plate number is 40, the tower top temperature is 75 ℃, and the reflux ratio is 0.3. And (3) taking the overhead gas of the dimethylamine separation tower as a heat source of a reboiler of the monomethylamine separation tower.
The results of this process for the separation of the monomethylamine dimethylamine starting material are given in the following table.
The total heat load of the reboiler of the monomethylamine separation tower is 995kW, the heat load of the gas phase at the top of the dimethylamine separation tower is 183kW, and the heat load can be saved by 18.4 percent by using the overhead gas of the dimethylamine separation tower as the heat source of the reboiler of the monomethylamine separation tower. Namely, the reboiler of the monomethylamine separation tower needs to supplement 812kW of heat load, and the rest is provided by the gas phase at the top of the second tower.
By the process, the high-purity monomethylamine and dimethylamine products can be obtained by mixing the monomethylamine and dimethylamine raw materials.
Example 3
By adopting the flow chart shown in fig. 1, the monomethylamine dimethylamine mixed raw material is subjected to energy-saving separation, the feeding amount is 3000kg/h, the feeding temperature is 50 ℃, and the feeding composition is shown in the following table.
The operation pressure of the monomethylamine separation tower T101 is 0.65MPa absolute pressure, the theoretical plate number is 72, the reflux ratio is 3.8, and the tower top temperature is 44 ℃.
The operating pressure of the dimethylamine separation tower T102 is absolute pressure 1.0MPa, the theoretical plate number is 20, the tower top temperature is 80 ℃, and the reflux ratio is 0.3. And (3) taking the overhead gas of the dimethylamine separation tower as a heat source of a reboiler of the monomethylamine separation tower.
The results of this process for the separation of the monomethylamine dimethylamine starting material are given in the following table.
The total heat load of the reboiler of the monomethylamine separation tower is 1272kW, the heat load of the gas phase at the top of the dimethylamine separation tower is 262kW, and the heat load can be saved by 20.6% by using the overhead gas of the dimethylamine separation tower as the heat source of the reboiler of the monomethylamine separation tower. Namely, 1010kW of heat load needs to be supplemented to a reboiler of the monomethylamine separation tower, and the rest is provided by a gas phase at the top of the second tower.
By the process, the high-purity monomethylamine and dimethylamine products can be obtained by mixing the monomethylamine and dimethylamine raw materials.
Comparative example
The existing process is adopted, a separation tower is used for separation, a methylamine product is extracted from the top of the tower, a dimethylamine product is extracted from the side line, and heavy components such as water and the like are extracted from the bottom of the tower.
The mixed raw material of monomethylamine dimethylamine was separated, with a feed rate of 3000kg/h, a feed temperature of 50 ℃ and a feed composition as shown in the following table.
The operating pressure of the separation tower is 0.65MPa absolute pressure, the number of theoretical plates is 72, and the temperature at the top of the tower is 44 ℃.
The comparative example was the same as example 3 in terms of the amount of monomethylamine and dimethylamine produced. Wherein, the total input heat load of the comparative example is 1526kW, which is 20 percent higher than the input total heat load 1272kW of the system of the example 3. The isolation results are shown in the following table:
as can be seen from the table, the comparative example product quality is close to that of example 3, but the heat load is 20% higher.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various changes and modifications can be made without departing from the inventive concept, and these changes and modifications are all within the scope of the present invention.
Claims (6)
1. An energy-saving separation process method of high-purity monomethylamine and dimethylamine is characterized in that: in the methylamine production process, a monomethylamine and dimethylamine mixed raw material dehydrated by a dehydrating tower is fed from the middle part of a monomethylamine separation tower, a monomethylamine product is rectified from the tower top and sent to a monomethylamine product tank for storage, dimethylamine mixed liquor at the tower bottom is sent to a dimethylamine separation tower, a dimethylamine product is rectified from the tower top and sent to the dimethylamine product tank, and a mixed liquor of recombinant water and methanol is discharged from the tower bottom; wherein, the overhead gas of the dimethylamine knockout tower is used as the heat source of a reboiler of the monomethylamine knockout tower.
2. The process according to claim 1, characterized in that: the operation pressure of the monomethylamine separation tower is 0.5-0.85 MPa absolute pressure, the number of theoretical plates is 50-100, the temperature of the top of the tower is 33-56 ℃, and the reflux ratio is 3.5-9.
3. The process according to claim 1, characterized in that: the operating pressure of the dimethylamine separation tower is 0.7-1.4 MPa absolute pressure, the number of theoretical plates is 5-50, the temperature of the top of the tower is 60-98 ℃, the reflux ratio is 0.005-2, and the operating pressure of the dimethylamine separation tower is higher than that of the monomethylamine separation tower.
4. The process according to claim 1, characterized in that: after heat exchange is carried out on the top gas of the dimethylamine separation tower serving as a heat source of a reboiler of the monomethylamine separation tower, one part of the top gas flows back to the dimethylamine separation tower, and the other part of the top gas is extracted as a product.
5. An energy-saving separation process device of high-purity monomethylamine and dimethylamine is characterized in that: the device comprises a methylamine separation tower and a dimethylamine separation tower, wherein an outlet at the top of the methylamine separation tower is sequentially connected with a methylamine separation tower condenser, a methylamine separation tower reflux tank and a methylamine separation tower reflux pump through an extraction pipeline; the first reboiler of a methylamine knockout tower is connected at the tower cauldron of methylamine knockout tower, the tower cauldron export of methylamine knockout tower is connected to the middle part feed inlet of dimethylamine knockout tower through adopting the pipeline, the top outlet of dimethylamine knockout tower connects gradually dimethylamine knockout tower condenser through adopting the pipeline, dimethylamine knockout tower reflux tank, dimethylamine knockout tower reflux pump, the outlet pipeline of dimethylamine knockout tower reflux pump divides into two routes, connect to the top reflux mouth of dimethylamine knockout tower on the same way, another way is connected to dimethylamine product jar through dimethylamine product condenser, connect dimethylamine knockout tower reboiler at the tower cauldron of dimethylamine knockout tower.
6. The apparatus of claim 5, wherein: the top outlet of the dimethylamine knockout tower is connected with the shell pass inlet of the dimethylamine knockout tower condenser, the shell pass outlet of the dimethylamine knockout tower condenser is connected with the dimethylamine knockout tower reflux tank, and the tube pass inlet and outlet of the dimethylamine knockout tower condenser are respectively connected with the tower kettle of the methylamine knockout tower and used as the second reboiler of the methylamine knockout tower.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB495516A (en) * | 1937-01-06 | 1938-11-15 | Roehm & Haas Co | Process for the separation of trimethylamine from mixtures with monomethylamine and dimethylamine |
| JPS57108041A (en) * | 1980-12-25 | 1982-07-05 | Mitsubishi Gas Chem Co Inc | Distilling and separating method of methylamine |
| CN1434023A (en) * | 2002-01-25 | 2003-08-06 | 三菱丽阳株式会社 | Process for preparing aminomethane |
| WO2010029087A1 (en) * | 2008-09-12 | 2010-03-18 | Basf Se | Method for the production of methylamines |
| CN111732515A (en) * | 2020-06-30 | 2020-10-02 | 北京诺维新材科技有限公司 | Method for separating methylamine |
| CN111792998A (en) * | 2020-06-30 | 2020-10-20 | 北京诺维新材科技有限公司 | Method for separating methylamine |
-
2020
- 2020-12-30 CN CN202011617156.6A patent/CN112745228A/en not_active Withdrawn
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB495516A (en) * | 1937-01-06 | 1938-11-15 | Roehm & Haas Co | Process for the separation of trimethylamine from mixtures with monomethylamine and dimethylamine |
| JPS57108041A (en) * | 1980-12-25 | 1982-07-05 | Mitsubishi Gas Chem Co Inc | Distilling and separating method of methylamine |
| CN1434023A (en) * | 2002-01-25 | 2003-08-06 | 三菱丽阳株式会社 | Process for preparing aminomethane |
| WO2010029087A1 (en) * | 2008-09-12 | 2010-03-18 | Basf Se | Method for the production of methylamines |
| CN111732515A (en) * | 2020-06-30 | 2020-10-02 | 北京诺维新材科技有限公司 | Method for separating methylamine |
| CN111792998A (en) * | 2020-06-30 | 2020-10-20 | 北京诺维新材科技有限公司 | Method for separating methylamine |
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Application publication date: 20210504 |