CN110551013A - energy recovery method of acrolein refining process - Google Patents
energy recovery method of acrolein refining process Download PDFInfo
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- CN110551013A CN110551013A CN201810542699.2A CN201810542699A CN110551013A CN 110551013 A CN110551013 A CN 110551013A CN 201810542699 A CN201810542699 A CN 201810542699A CN 110551013 A CN110551013 A CN 110551013A
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- material flow
- heat exchanger
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- tower
- acrolein
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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
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention relates to an energy recovery method of an acrolein refining process, which comprises the following steps: s1, introducing a reaction product generated by catalytic oxidation of propylene into an absorption tower to form a first material flow containing acrolein at the bottom of the absorption tower, introducing the first material flow into a light component removal tower after the first material flow is heated by a first heat exchanger, forming a second material flow containing acrolein at the bottom of the light component removal tower, introducing the second material flow into a purification tower after the second material flow is heated by a second heat exchanger to purify the acrolein in the second material flow, and forming a third material flow at the bottom of the purification tower; s2, introducing the third material flow into the second heat exchanger and the first heat exchanger respectively to provide heat for the second material flow and the first material flow. The first material flow and the second material flow with lower temperature exchange heat with the third material flow with higher temperature, so that the energy carried by the third material flow is fully utilized, and the energy waste caused by directly cooling the third material flow is avoided. By absorbing the heat in the third stream, the energy consumption of the light component removal tower and the purification tower is reduced.
Description
Technical Field
The invention relates to an energy recovery method, in particular to an energy recovery method of an acrolein refining process.
Background
Acrolein is an important organic chemical raw material with wide application. At present, the method is mainly used for preparing the methionine serving as an animal feed additive, and is also used for preparing glycerol, glutaraldehyde, allyl alcohol, 1,2, 6-hexanetriol, 2, 3-dibromopropionaldehyde and a water treatment agent, modifying certain polymers, and widely applying the method to the feed industry, oil and gas exploitation, papermaking, water treatment, medicine industry and other aspects. The synthesis method of acrolein mainly comprises a propylene oxidation method, a formaldehyde-acetaldehyde gas phase condensation method, a propane catalytic oxidation method, a glycerin dehydration method, an aldol condensation method, a propylene ether pyrolysis method, an allyl alcohol oxidation method and the like, and the propylene oxidation method is the main method for industrially producing acrolein at present. In the prior art, after an acrolein refining process is finished, a liquid phase material flow at the bottom of a purification tower is directly cooled by a cooler and then is sent into an absorption tower as washing water to absorb a product generated after catalytic oxidation of propylene. Therefore, in the prior art, the method of directly cooling the liquid phase material flow at the bottom of the purification tower is adopted, so that the heat in the liquid phase material flow at the bottom of the purification tower is not fully utilized, energy is wasted, a large amount of chilled water for cooling is consumed, the cost is further increased in the acrolein refining process, and the overall benefit of an enterprise is influenced.
Disclosure of Invention
The invention aims to provide an energy recovery method for an acrolein refining process, which improves the energy utilization efficiency in the acrolein refining process.
In order to achieve the above object, the present invention provides an energy recovery method of an acrolein refining process, comprising:
S1, introducing a reaction product generated by catalytic oxidation of propylene into an absorption tower to form a first material flow containing acrolein at the bottom of the absorption tower, introducing the first material flow into a light component removal tower after the first material flow is heated by a first heat exchanger, forming a second material flow containing acrolein at the bottom of the light component removal tower, introducing the second material flow into a purification tower after the second material flow is heated by a second heat exchanger to purify the acrolein in the second material flow, and forming a third material flow at the bottom of the purification tower;
S2, introducing the third material flow into the second heat exchanger and the first heat exchanger respectively to provide heat for the second material flow and the first material flow.
According to an aspect of the invention, step S2 includes:
S21, introducing the third material flow into the second heat exchanger to exchange heat with the second material flow;
S22, introducing the third material flow passing through the second heat exchanger into the first heat exchanger to exchange heat with the first material flow.
according to an aspect of the invention, further comprising:
s23, introducing the third material flow passing through the first heat exchanger into a third heat exchanger for cooling, and then sending the cooled third material flow into the absorption tower to absorb the reaction product to form the first material flow.
according to one aspect of the present invention, in step S22, the number of the first heat exchangers is two, and the first heat exchangers are sequentially arranged in series.
According to one aspect of the invention, the temperature of the first stream after passing through the first heat exchanger is increased by 35 ℃ to 45 ℃ in step S22.
According to one aspect of the invention, in step S21, the temperature of the second stream increases by 25 ℃ to 35 ℃ after passing through the second heat exchanger.
According to one aspect of the invention, the temperature of the third stream after passing through the third heat exchanger is less than 10 ℃ in step S23.
According to an aspect of the invention, in step S23, the third stream contains acrylic acid, and the mass percentage of acrylic acid is 1% to 8%.
according to one scheme of the invention, the first material flow and the second material flow with lower temperature exchange heat with the third material flow with higher temperature, so that the energy carried by the third material flow is fully utilized, and the energy waste caused by directly cooling the third material flow is avoided. Meanwhile, by absorbing the heat in the third stream, the heating time of the first stream and the second stream in the light component removal tower and the purification tower respectively is saved, and the energy consumption of the light component removal tower and the purification tower is reduced. Through the process, the heating of the first material flow and the second material flow and the refrigerating effect of the third material flow are achieved respectively, the energy utilization efficiency is optimized, the energy is saved, and the production cost is reduced.
according to one scheme of the invention, the two first heat exchangers are arranged in series, so that the energy carried by the third material flow is fully absorbed by the first material flow, the temperature of the first material flow can be increased by 35-45 ℃, the temperature of the third material flow is effectively reduced, the use amount of cooling water when the third material flow passes through the third heat exchanger is reduced, the energy is saved, the cooling time of the third material flow is reduced, and the production cost is effectively saved.
Drawings
Fig. 1 schematically shows a block diagram of an energy recovery system according to an embodiment of the invention.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments will be briefly described below. It is obvious that the drawings in the following description are only some embodiments of the invention, and that for a person skilled in the art, other drawings can be derived from them without inventive effort.
In describing embodiments of the present invention, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in an orientation or positional relationship that is based on the orientation or positional relationship shown in the associated drawings, which is for convenience and simplicity of description only, and does not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and thus, the above-described terms should not be construed as limiting the present invention.
The present invention is described in detail below with reference to the drawings and the specific embodiments, which are not repeated herein, but the embodiments of the present invention are not limited to the following embodiments.
According to one embodiment of the present invention, a method of energy recovery for an acrolein refining process of the present invention comprises:
S1, introducing a reaction product generated by catalytic oxidation of propylene into an absorption tower 1 to form a first material flow A containing acrolein at the bottom of the tower, introducing the first material flow A into a light component removal tower 3 after being heated by a first heat exchanger 2, forming a second material flow B containing acrolein at the bottom of the light component removal tower 3, introducing the second material flow B into a purification tower 5 after being heated by a second heat exchanger 4 to purify the acrolein in the second material flow B, and forming a third material flow C at the bottom of the tower;
S2, introducing the third stream C into a second heat exchanger 4 and a first heat exchanger 2 respectively to provide heat for a second stream B and a first stream A.
As shown in fig. 1, according to one embodiment of the present invention, the energy recovery method of the present invention is realized by a purification system in an acrolein purification process. In the present embodiment, the purification system includes: the device comprises an absorption tower 1, a first heat exchanger 2, a lightness-removing tower 3, a second heat exchanger 4 and a purifying tower 5. in the embodiment, a discharge hole at the bottom of the absorption tower 1 is communicated with the first heat exchanger 2 through a pipeline, and the first heat exchanger 2 is communicated with a feed hole of the lightness-removing tower 3 through a pipeline. The discharge hole at the bottom of the light component removal tower 3 is communicated with the second heat exchanger 4 through a pipeline. The second heat exchanger 4 is communicated with the feed inlet of the purifying tower 5 through a pipeline. The discharge hole at the bottom of the purification tower 5 is communicated with the second heat exchanger 4 and the first heat exchanger 2 in sequence through pipelines.
As shown in fig. 1, according to one embodiment of the present invention, in step S1, the inlet of the absorber 1 receives the reaction product generated by the catalytic oxidation of propylene. In the present embodiment, the reaction product contains acrolein, acrylic acid produced by a side reaction, and the like. Acrolein and the like in the reaction product are absorbed by the absorbent in the absorption tower 1 to become a first stream A containing acrolein at the bottom of the absorption tower 1. The first material flow A is conveyed to the first heat exchanger 2 through a pipeline at the bottom of the absorption tower 1, and the temperature of the first material flow A is increased after the heat exchange effect of the first heat exchanger 2. In the embodiment, the temperature of the first material flow A after passing through the first heat exchanger is increased by 35-45 ℃, and the temperature of the first material flow A is increased by 35-45 ℃, so that the light components in the first material flow A can be effectively separated in the light component removal tower 3, the energy requirement in the subsequent light component removal tower 3 during separation operation is saved, the energy utilization rate is improved, and the cost is saved.
In the present embodiment, the first stream a after the temperature increase is sent to the lightness-removing column 3 through a pipeline. After removing the light components in the first stream A in the light component removal tower 3, a second stream B containing acrolein is formed at the bottom of the light component removal tower 3. The second stream B is conveyed to a second heat exchanger 4 through a pipeline at the bottom of the lightness-removing tower 3, and the temperature of the second stream B is increased after the heat exchange effect of the second heat exchanger 4. In this embodiment, the temperature of the second stream B after passing through the second heat exchanger 4 is increased by 25 ℃ to 35 ℃. The second stream B is raised by 25-35 ℃, so that the acrolein in the second stream B can be effectively separated in the purification tower 5, the energy requirement in the subsequent separation operation in the purification tower 5 is saved, the energy utilization rate is improved, and the cost is saved.
As shown in fig. 1, according to one embodiment of the present invention, the first heat exchanger 2 is provided with two. In the present embodiment, two first heat exchangers 2 are provided in series between the absorption column 1 and the light ends removal column 3. The first material flow A sequentially enters the lightness-removing tower 3 through two first heat exchangers 2 through a pipeline.
as shown in fig. 1, according to one embodiment of the present invention, in step S2, the third stream C is introduced into the second heat exchanger 4 and the first heat exchanger 2 to provide heat for the second stream B and the first stream a, respectively. In the present embodiment, the present invention includes:
S21, introducing the third stream C into a second heat exchanger 4 to exchange heat with the second stream B. In this embodiment, after the purification of acrolein in the second stream B is completed in the purification column 5, a third stream C having a higher temperature is produced. The third flow C at the bottom of the purifying tower 5 enters a second heat exchanger 4 through a pipeline, the heat exchange between the third flow C and the second flow B is completed in the second heat exchanger 4, and the temperature of the third flow C is reduced by 28-32 ℃.
S22, introducing the third material flow C passing through the second heat exchanger 4 into the first heat exchanger 2 to exchange heat with the first material flow A. In the present embodiment, the third stream C which has passed through the second heat exchanger 4 is passed on via a line to the first heat exchanger 2. In this embodiment, the third stream C is required to heat the first stream a sequentially through two first heat exchangers 2 in series. In this embodiment, the third stream C is fed from the first heat exchanger 2 on the side close to the lightness-removing column 3. After completing the heat exchange of the third stream C with the first stream a in both first heat exchangers 2, the temperature of the third stream C is reduced by 38 ℃ to 42 ℃.
As shown in fig. 1, according to an embodiment of the present invention, the refining system of the present invention further includes: a third heat exchanger 6. In the present embodiment, the third heat exchanger 6 communicates with the first heat exchanger 2 through a pipe, and communicates with the absorbent feed port of the absorption column 1 through a pipe. In step S2, the method further includes:
S23, introducing the third material flow C after passing through the first heat exchanger 2 into a third heat exchanger 6 for cooling, and then sending the cooled third material flow C into an absorption tower 1 to absorb reaction products to form a first material flow A. In this embodiment, the third stream C is introduced into the third heat exchanger 6 and then subjected to heat exchange to lower the temperature of the third stream C to a temperature required for absorbing the reaction product. In this embodiment, let in external refrigerated water to cooling down third commodity circulation C in the third heat exchanger 6, thereby effectively guarantee that third commodity circulation C is effectively cooled down through adopting the refrigerated water, guaranteed that third commodity circulation C can reach the best absorption effect after sending into absorption tower 1. In this embodiment, the temperature of the third stream C after passing through the third heat exchanger 6 is below 10 ℃. The temperature of the third stream C is reduced to below 10 ℃ so as to ensure the absorption of acrolein in the reaction product and effectively improve the absorption efficiency.
In this embodiment, the third stream contains acrylic acid, and the mass percent of acrylic acid is 1% to 8%. The presence of the above-mentioned percentages by mass of acrylic acid in the third stream further facilitates the absorption of acrolein in the reaction product in the absorption column 1. Thus, feeding the third stream C into the absorption column 1 ensures that the third stream C is fed to sufficiently absorb acrolein in the reaction product and to ensure that the third stream as an absorbent is saturated in acrolein content, thereby reducing the number of cycles of the absorbent (i.e., the third stream) and further reducing the energy consumption of the refining system of the present invention.
According to another embodiment of the present invention, in step S2, the third stream C may provide heat separately to the second heat exchanger 4 and the first heat exchanger 2, respectively, i.e. the second heat exchanger 4 and the first heat exchanger 2 do not need to be in pipe communication. In the present embodiment, after the third stream C is introduced into the second heat exchanger 4 to exchange heat with the second stream B, the third stream C is directly conveyed to the third heat exchanger 6 to be cooled, and then the cooled third stream C is conveyed to the absorption tower 1. Meanwhile, after the third stream C is introduced into the first heat exchanger 2 to exchange heat with the first stream a, the third stream C is directly conveyed to the third heat exchanger 6 to be cooled, and then the cooled third stream C is conveyed to the absorption tower 1.
According to the method, the first material flow A and the second material flow B with lower temperature exchange heat with the third material flow C with higher temperature, so that the energy carried by the third material flow C is fully utilized, and the energy waste caused by directly cooling the third material flow C is avoided. Meanwhile, by absorbing the heat in the third stream C, the heating time of the first stream A and the second stream B in the light component removal tower 3 and the purification tower 5 respectively is saved, and the energy consumption of the light component removal tower 3 and the purification tower 5 is reduced. Through the process, the heating effect of the first material flow A and the second material flow B and the refrigerating effect of the third material flow C are achieved respectively, the energy utilization efficiency is optimized, the energy is saved, and the production cost is reduced.
According to the method, the first heat exchangers 2 are arranged in two and are mutually connected in series, so that the energy carried by the third material flow A is fully absorbed by the first material flow A, the temperature of the first material flow A can be increased by 35-45 ℃, the temperature of the third material flow A is effectively reduced, the use amount of cooling water when the third material flow A passes through the third heat exchanger 6 is reduced, energy is saved, the cooling time of the third material flow A is reduced, and the production cost is effectively saved.
the above description is only one embodiment of the present invention, and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. a method of energy recovery for an acrolein refining process comprising:
s1, introducing a reaction product generated by catalytic oxidation of propylene into an absorption tower to form a first material flow containing acrolein at the bottom of the absorption tower, introducing the first material flow into a light component removal tower after the first material flow is heated by a first heat exchanger, forming a second material flow containing acrolein at the bottom of the light component removal tower, introducing the second material flow into a purification tower after the second material flow is heated by a second heat exchanger to purify the acrolein in the second material flow, and forming a third material flow at the bottom of the purification tower;
S2, introducing the third material flow into the second heat exchanger and the first heat exchanger respectively to provide heat for the second material flow and the first material flow.
2. The energy recovery method according to claim 1, wherein step S2 includes:
S21, introducing the third material flow into the second heat exchanger to exchange heat with the second material flow;
S22, introducing the third material flow passing through the second heat exchanger into the first heat exchanger to exchange heat with the first material flow.
3. The energy recovery method of claim 2, further comprising:
S23, introducing the third material flow passing through the first heat exchanger into a third heat exchanger for cooling, and then sending the cooled third material flow into the absorption tower to absorb the reaction product to form the first material flow.
4. The energy recovery method of claim 2, wherein in step S22, the first heat exchangers are two and are arranged in series in sequence.
5. The energy recovery process of claim 2 or 4, wherein the temperature of the first stream after passing through the first heat exchanger is increased by 35 ℃ to 45 ℃ in step S22.
6. The energy recovery method of claim 2, wherein in step S21, the temperature of the second stream after passing through the second heat exchanger is increased by 25 ℃ to 35 ℃.
7. The energy recovery method of claim 3, wherein the temperature of the third stream after passing through the third heat exchanger is less than 10 ℃ in step S23.
8. The energy recovery method according to claim 3, wherein in step S23, the third stream contains acrylic acid, and the mass percentage of acrylic acid is 1% -8%.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201810542699.2A CN110551013A (en) | 2018-05-30 | 2018-05-30 | energy recovery method of acrolein refining process |
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| CN201810542699.2A CN110551013A (en) | 2018-05-30 | 2018-05-30 | energy recovery method of acrolein refining process |
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| CN110551013A true CN110551013A (en) | 2019-12-10 |
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| CN201810542699.2A Pending CN110551013A (en) | 2018-05-30 | 2018-05-30 | energy recovery method of acrolein refining process |
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Application publication date: 20191210 |