CN113248358A - Method and equipment for producing propionaldehyde through ethylene hydroformylation gas phase circulation - Google Patents
Method and equipment for producing propionaldehyde through ethylene hydroformylation gas phase circulation Download PDFInfo
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- NBBJYMSMWIIQGU-UHFFFAOYSA-N Propionic aldehyde Chemical compound CCC=O NBBJYMSMWIIQGU-UHFFFAOYSA-N 0.000 title claims abstract description 276
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 135
- 239000005977 Ethylene Substances 0.000 title claims abstract description 135
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N butyric aldehyde Natural products CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 title claims abstract description 105
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000007037 hydroformylation reaction Methods 0.000 title claims abstract description 15
- 238000000926 separation method Methods 0.000 claims abstract description 79
- 238000010992 reflux Methods 0.000 claims abstract description 43
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 239000000463 material Substances 0.000 claims abstract description 33
- 239000000047 product Substances 0.000 claims abstract description 29
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 13
- 239000007791 liquid phase Substances 0.000 claims abstract description 13
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 13
- 238000001816 cooling Methods 0.000 claims abstract description 12
- 239000002994 raw material Substances 0.000 claims abstract description 11
- 230000008569 process Effects 0.000 claims abstract description 10
- 239000006227 byproduct Substances 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 11
- 230000006835 compression Effects 0.000 claims description 7
- 238000007906 compression Methods 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 238000006073 displacement reaction Methods 0.000 claims description 3
- 239000012808 vapor phase Substances 0.000 claims description 2
- 239000012071 phase Substances 0.000 abstract description 4
- 239000011541 reaction mixture Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 25
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 description 4
- 238000007872 degassing Methods 0.000 description 3
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 235000019260 propionic acid Nutrition 0.000 description 2
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- PTBDIHRZYDMNKB-UHFFFAOYSA-N 2,2-Bis(hydroxymethyl)propionic acid Chemical compound OCC(C)(CO)C(O)=O PTBDIHRZYDMNKB-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- IAYPIBMASNFSPL-UHFFFAOYSA-N Ethylene oxide Chemical compound C1CO1 IAYPIBMASNFSPL-UHFFFAOYSA-N 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000000539 dimer Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000000819 phase cycle Methods 0.000 description 1
- -1 polyethylene Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 239000013638 trimer Substances 0.000 description 1
- QXJQHYBHAIHNGG-UHFFFAOYSA-N trimethylolethane Chemical compound OCC(C)(CO)CO QXJQHYBHAIHNGG-UHFFFAOYSA-N 0.000 description 1
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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
- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
- C07C45/505—Asymmetric hydroformylation
-
- 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
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method and a device for producing propionaldehyde by ethylene hydroformylation gas phase circulation, wherein the method comprises the following steps: s1, introducing raw material ethylene and synthesis gas into a propionaldehyde reactor to perform hydroformylation reaction to generate a first material flow containing propionaldehyde and a byproduct; s2, sending the first material flow to an ethylene separation tower, and separating a second material flow containing propionaldehyde; s3, cooling the second stream to obtain a third stream which contains propionaldehyde and is in a liquid phase, and sending the third stream to a reflux tank of the ethylene separation tower; and S4, returning a part of the third material flow extracted from the reflux tank of the ethylene separation tower to the ethylene separation tower as reflux, sending the other part of the third material flow to a stripping tower for treatment, and obtaining a propionaldehyde product at the tower kettle of the stripping tower. The propionaldehyde product can be separated from the reaction mixture as quickly as possible by adopting a shorter process, so that the purity of the finally obtained propionaldehyde product and the conversion rate of the raw material are higher.
Description
Technical Field
The invention relates to the field of chemical industry, in particular to a method and equipment for producing propionaldehyde through ethylene hydroformylation gas phase circulation.
Background
Propionaldehyde has wide application in the field of chemical production, and is a main raw material for producing chemicals such as propionic acid, n-propanol, trimethylolethane, dimethylolpropionic acid and the like; meanwhile, the product can be used as a polymerization inhibitor in the production of polyethylene and can also be used in the fields of synthetic resin, synthetic rubber and the like; propionaldehyde is also useful as an antioxidant, a promoter, and the like. At present, the industrial production method of propionaldehyde mainly comprises the following steps: ethylene hydroformylation, propanol oxidation, ethylene oxide isomerization, acrolein hydrogenation, and the by-product of propylene oxidation to acetone. Among them, the ethylene hydroformylation method is the most widely industrially used method because of low energy consumption and stable operation.
However, in the existing method, the route from the reaction of the propionaldehyde to the final product is long, and the propionaldehyde is easy to polymerize to generate heavy components such as dimer, trimer and the like, so that the process separation difficulty is increased, and the yield of the propionaldehyde is reduced.
Disclosure of Invention
The invention aims to provide a method and equipment for producing propionaldehyde by ethylene hydroformylation gas phase circulation.
In order to achieve the above object, the present invention provides a method for producing propionaldehyde by ethylene hydroformylation gas phase cycle, comprising:
s1, introducing raw material ethylene and synthesis gas into a propionaldehyde reactor to perform hydroformylation reaction to generate a first material flow containing propionaldehyde and a byproduct;
s2, sending the first material flow to an ethylene separation tower, and separating a second material flow containing propionaldehyde;
s3, cooling the second stream to obtain a third stream which contains propionaldehyde and is in a liquid phase, and sending the third stream to a reflux tank of the ethylene separation tower;
and S4, returning a part of the third material flow extracted from the reflux tank of the ethylene separation tower to the ethylene separation tower as reflux, sending the other part of the third material flow to a stripping tower for treatment, and obtaining a propionaldehyde product at the tower kettle of the stripping tower.
According to one aspect of the invention, a catalyst is disposed in the propanal reactor;
the reaction temperature of the propionaldehyde reactor is 70-110 ℃, and the reaction pressure is 1.0-1.8 MPa.
According to one aspect of the invention, in step S3, the step of cooling the second stream to obtain a third stream comprising propanal and in liquid phase, the second stream is passed through a propanal cooler and a propanal aftercooler to obtain the third stream.
According to an aspect of the present invention, in step S3, in the step of cooling the second stream to obtain a third stream containing propionaldehyde and in a liquid phase, the uncooled gas in the second stream is returned to the propionaldehyde reactor for continuing the reaction after being compressed and pressurized by the recycle ethylene compressor.
According to one aspect of the invention, the step of sending another part to a stripper column for treatment and obtaining a propanal product in the bottom of the stripper column in step S4 comprises:
s41, adding the third material flow from the top of the stripping tower;
and S42, adding synthesis gas from a tower kettle of the stripping tower, stripping ethylene dissolved in the third material flow out, and then sending the ethylene to the propionaldehyde reactor to participate in reaction.
According to one aspect of the invention, the pressure of the ethylene separation tower is 0.6-1.4 MPa, and the reflux ratio is 0.02-1.
According to one aspect of the invention, the ethylene separation column is a tray column or a packed column, preferably a packed column.
According to one aspect of the invention, the compression ratio of the recycle ethylene compressor is 1.2-3.
According to one aspect of the invention, the recycle ethylene compressor is a positive displacement compressor or a centrifugal compressor.
According to one aspect of the invention, the ethylene splitter bottoms liquid stream is returned to the propanal reactor.
To achieve the above object, the present invention provides an apparatus for the aforementioned method, comprising: the system comprises a propionaldehyde reactor, an ethylene separation tower connected with the propionaldehyde reactor through a pipeline, a propionaldehyde cooler connected with the ethylene separation tower through a pipeline, a propionaldehyde after-cooler connected with the propionaldehyde cooler through a pipeline, a circulating ethylene compressor respectively connected with the propionaldehyde after-cooler and the propionaldehyde reactor through pipelines, an ethylene separation tower reflux tank, an ethylene separation tower reflux pump and a stripping tower;
the ethylene separation tower reflux tank is respectively connected with the propionaldehyde cooler, the propionaldehyde after-cooler and the ethylene separation tower reflux pump through pipelines;
the ethylene separation tower reflux pump is respectively connected with the ethylene separation tower and the stripping tower through pipelines;
the stripper column is connected to the propanal reactor via a line.
According to one embodiment of the present invention, the propionaldehyde product can be separated from the reaction mixture as quickly as possible by using a shorter process, resulting in a higher purity of the propionaldehyde product and higher conversion of the starting material.
According to one scheme of the invention, the purity of the finally obtained propionaldehyde product is more than or equal to 99.5 percent, and the ethylene conversion rate is more than or equal to 92 percent.
According to one scheme of the invention, the process flow is simple, the separation of unreacted ethylene and the product propionaldehyde is realized by arranging the ethylene separation tower, the generated propionaldehyde product and the unreacted ethylene are quickly separated, the generation of a propionaldehyde polymer is effectively prevented, the continuous, stable and efficient operation of a system is ensured, and the energy consumption is low.
According to the scheme of the invention, the materials which are not completely reacted are recycled, so that the material conversion rate of the invention is effectively improved, and the resources and the cost are saved.
Drawings
FIG. 1 is a block diagram schematically representing the steps of a method according to one embodiment of the invention;
fig. 2 is a block diagram schematically showing an apparatus according to an embodiment of the present 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.
As shown in fig. 1, according to one embodiment of the present invention, a method for vapor phase recycle production of propionaldehyde by hydroformylation of ethylene comprises:
s1, introducing raw material ethylene and synthesis gas into a propionaldehyde reactor to perform hydroformylation reaction to generate a first material flow containing propionaldehyde and a byproduct;
s2, sending the first material flow to an ethylene separation tower, and separating a second material flow containing propionaldehyde;
s3, cooling the second stream to obtain a third stream which contains propionaldehyde and is in a liquid phase, and sending the third stream to a reflux tank of the ethylene separation tower;
s4, returning a part of the third material flow extracted from the reflux tank of the ethylene separation tower to the ethylene separation tower as reflux through a reflux pump of the ethylene separation tower, and sending the other part of the third material flow to the stripping tower for treatment and obtaining a propionaldehyde product at the tower kettle of the stripping tower.
As shown in fig. 2, in step S1, raw material ethylene and synthesis gas are introduced into a propionaldehyde reactor to perform hydroformylation reaction, so as to generate a first stream containing propionaldehyde and byproducts, wherein a catalyst is disposed in the propionaldehyde reactor. In this embodiment, ethylene is hydroformylated with synthesis gas under the catalytic action of the catalyst. The first stream produced by the reaction is a mixed stream comprising propionaldehyde and by-products of ethane, propionic acid, and the like. In the embodiment, the reaction temperature of the propionaldehyde reactor is 70-110 ℃, and the reaction pressure is 1.0-1.8 MPa.
As shown in figure 2, step s2. the first stream is sent to an ethylene separation column, in a step of separating a second stream comprising propanal, according to one embodiment of the present invention. The first material flow is carried to an ethylene separation tower by a circulating gas through a pipeline between a propionaldehyde reactor and the ethylene separation tower, unreacted gases such as ethylene, synthetic gas and the like are separated from a product propionaldehyde in the ethylene separation tower, and a second material flow mainly containing components such as ethylene, synthetic gas, propionaldehyde and the like is extracted from the tower top.
As shown in fig. 2, in step S3, the second stream is cooled to obtain a third stream containing propanal and in liquid phase, and the third stream is obtained by passing the second stream through a propanal cooler 103 and a propanal aftercooler 104. In this embodiment, the second stream is cooled by the propanal cooler 103 and the propanal aftercooler 104, and further, the third stream is composed of two liquid phase streams sent out from the propanal cooler 103 and the propanal aftercooler 104, wherein the second stream first enters the propanal cooler 103 after being extracted from the top of the ethylene separation tower 102, the liquid phase stream obtained after the cooling treatment by the propanal cooler 103 is a part of the third stream, and meanwhile, after the first cooling by the propanal cooler 103, the part which is not condensed enters the propanal aftercooler 104 through a pipeline, and the liquid phase stream obtained by the second cooling in the propanal aftercooler 104 is the other part of the third stream. In this embodiment, the third stream taken in propionaldehyde cooler 103 and propionaldehyde aftercooler 104 is sent collectively to ethylene separation column reflux drum 106.
As shown in fig. 2, in step S3, in the step of cooling the second stream to obtain a third stream containing propionaldehyde and in liquid phase, the uncooled gas in the second stream is compressed and pressurized by the recycle ethylene compressor 105, and then returned to the propionaldehyde reactor 101 for further reaction.
As shown in fig. 2, according to an embodiment of the present invention, step s4. the third stream withdrawn from the reflux drum 106 of the ethylene separation column is returned to the ethylene separation column 102 as reflux via a part of the reflux pump 107 of the ethylene separation column, and the other part is sent to the stripper 108 for treatment and obtaining propionaldehyde product at the bottom of the stripper 108. In this embodiment, the step of sending the other part to the stripper 108 for treatment and obtaining the propanal product in the bottom of the stripper 108 comprises:
s41, adding a third material flow from the top of the stripping tower 108;
and S42, adding synthesis gas from the tower bottom of the gas stripping 108, stripping ethylene dissolved in the third stream, and then sending the ethylene to the propionaldehyde reactor 101 for reaction.
As shown in FIG. 2, according to one embodiment of the present invention, the pressure of the ethylene separation column 102 is 0.6 to 1.4MPa, and the reflux ratio is 0.02 to 1. In the present embodiment, the ethylene separation column 102 is a tray column or a packed column, and a packed column is preferable.
As shown in FIG. 2, according to one embodiment of the present invention, the recycle ethylene compressor 105 has a compression ratio of 1.2 to 3. In this embodiment, the recycle ethylene compressor 105 is a positive displacement compressor or a centrifugal compressor.
As shown in fig. 2, according to one embodiment of the present invention, the bottom liquid stream (containing mostly propanal and heavy components) of the ethylene splitter 102 is returned to the propanal reactor. In this embodiment, the propanal reactor is periodically purged to prevent the accumulation of heavies.
To further illustrate the advantages of the present invention, a number of examples are set forth.
Example 1
According to the method, raw materials of ethylene and synthesis gas are reacted in an environment that a propionaldehyde reactor 101 is at a reaction temperature of 80-90 ℃ and a reaction pressure of 1.2-1.3 MPa, after the reaction, the product is sent to an ethylene separation tower 102 for gas-liquid separation, the pressure of the ethylene separation tower 102 is 1.0MPa, the reflux ratio is 0.02, uncondensed ethylene gas extracted from the top of the ethylene separation tower 102 needs to be pressurized by a circulating ethylene compressor 105, the compression ratio of the circulating ethylene compressor 105 is 1.5, one part of condensed third material flow containing propionaldehyde is returned to the ethylene separation tower 102 as reflux, the other part of condensed third material flow is sent to a stripper 108 as extracted liquid, and after degassing in the stripper 108, a propionaldehyde product is obtained at the bottom of the tower, wherein the purity of the propionaldehyde product is 99.6%, and the ethylene conversion rate is 90%.
Example 2
According to the method, raw materials of ethylene and synthesis gas are reacted in an environment that a propionaldehyde reactor 101 is at a reaction temperature of 90-100 ℃ and a reaction pressure of 1.0-1.1 MPa, after the reaction, the product is sent to an ethylene separation tower 102 for gas-liquid separation, the pressure of the ethylene separation tower 102 is 0.9MPa, the reflux ratio is 0.1, the uncondensed ethylene gas extracted from the top of the ethylene separation tower 102 needs to be pressurized by a circulating ethylene compressor 105, the compression ratio of the circulating ethylene compressor 105 is 1.2, one part of a condensed third material flow containing propionaldehyde is returned to the ethylene separation tower 102 as reflux, the other part of the condensed third material flow is sent to a stripper 108 as extracted liquid, and after degassing is carried out in the stripper 108, a propionaldehyde product is obtained at the tower bottom, wherein the purity of the propionaldehyde product is 99.5%, and the ethylene conversion rate is 92%.
Example 3
According to the method, raw materials of ethylene and synthesis gas are reacted in an environment with a propionaldehyde reactor 101 at a reaction temperature of 100-110 ℃ and a pressure of 1.7-1.8 MPa, after the reaction, the product is sent to an ethylene separation tower 102 for gas-liquid separation, the pressure of the ethylene separation tower 102 is 1.4MPa, the reflux ratio is 0.5, uncondensed ethylene gas extracted from the top of the ethylene separation tower 102 needs to be pressurized by a circulating ethylene compressor 105, the compression ratio of the circulating ethylene compressor 105 is 3, one part of a condensed third stream containing propionaldehyde is returned to the ethylene separation tower 102 as reflux, the other part of the condensed third stream is sent to a stripper 108 as an extracted liquid, and after degassing is carried out in the stripper 108, a propionaldehyde product is obtained at the bottom of the stripper 108, wherein the purity of the propionaldehyde product is 99%, and the ethylene conversion rate is 93%.
Example 4
According to the method, raw materials of ethylene and synthesis gas are reacted in an environment that a propionaldehyde reactor 101 is at a reaction temperature of 70-80 ℃ and a reaction pressure of 1.0-1.1 MPa, after the reaction, the product is sent to an ethylene separation tower 102 for gas-liquid separation, the pressure of the ethylene separation tower 102 is 0.6MPa, the reflux ratio is 1, uncondensed ethylene gas extracted from the top of the ethylene separation tower 102 needs to be pressurized by a circulating ethylene compressor 105, the compression ratio of the circulating ethylene compressor 105 is 2, one part of a condensed third stream containing propionaldehyde is returned to the ethylene separation tower 102 as reflux, the other part of the condensed third stream is sent to a stripper 108 as an extracted liquid, and after the propionaldehyde 108 is degassed, a product is obtained at the tower bottom, the purity of the product is 99.4%, and the ethylene conversion rate is 80%.
As shown in fig. 1, according to an embodiment of the present invention, an apparatus of the present invention for the foregoing method includes: propionaldehyde reactor 101, ethylene separation tower 102 connected with propionaldehyde reactor 101 through the pipeline, propionaldehyde cooler 103 connected with ethylene separation tower 102 through the pipeline, propionaldehyde after-cooler 104 connected with propionaldehyde cooler 103 through the pipeline, circulating ethylene compressor 105 connected with propionaldehyde after-cooler 104 and propionaldehyde reactor 101 respectively through the pipeline, ethylene separation tower reflux tank 106, ethylene separation tower reflux pump 107, stripper 108. In the present embodiment, the ethylene separation column reflux drum 106 is connected to the propionaldehyde cooler 103, the propionaldehyde after-cooler 104, and the ethylene separation column reflux pump 107 through pipelines, respectively; the ethylene separation tower reflux pump 107 is respectively connected with the ethylene separation tower 102 and the stripping tower 108 through pipelines; the stripper 108 is connected to the propanal reactor 101 via a line.
The foregoing is merely exemplary of particular aspects of the present invention and devices and structures not specifically described herein are understood to be those of ordinary skill in the art and are intended to be implemented in such conventional ways.
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 (11)
1. A process for the vapor phase recycle production of propanal by the hydroformylation of ethylene comprising:
s1, introducing raw material ethylene and synthesis gas into a propionaldehyde reactor to perform hydroformylation reaction to generate a first material flow containing propionaldehyde and a byproduct;
s2, sending the first material flow to an ethylene separation tower, and separating a second material flow containing propionaldehyde;
s3, cooling the second stream to obtain a third stream which contains propionaldehyde and is in a liquid phase, and sending the third stream to a reflux tank of the ethylene separation tower;
and S4, returning a part of the third material flow extracted from the reflux tank of the ethylene separation tower to the ethylene separation tower as reflux, sending the other part of the third material flow to a stripping tower for treatment, and obtaining a propionaldehyde product at the tower kettle of the stripping tower.
2. The process of claim 1, wherein the propanal reactor has a catalyst disposed therein;
the reaction temperature of the propionaldehyde reactor is 70-110 ℃, and the reaction pressure is 1.0-1.8 MPa.
3. The process of claim 1, wherein in step S3, the step of cooling the second stream to obtain a third stream comprising propanal and in liquid phase, the second stream is passed through a propanal cooler and a propanal aftercooler to obtain the third stream.
4. The method according to claim 3, wherein in step S3, in the step of cooling the second stream to obtain a third stream containing propionaldehyde and in liquid phase, the uncooled gas in the second stream is returned to the propionaldehyde reactor for continuous reaction after being compressed and pressurized by a recycle ethylene compressor.
5. The process of any one of claims 1 to 4, wherein in step S4, the other part is sent to a stripper column for treatment and obtaining a propanal product in the stripper column bottom, comprising:
s41, adding the third material flow from the top of the stripping tower;
and S42, adding synthesis gas from a tower kettle of the stripping tower, stripping ethylene dissolved in the third material flow out, and then sending the ethylene to the propionaldehyde reactor to participate in reaction.
6. The method of claim 1, wherein the pressure of the ethylene separation column is 0.6 to 1.4MPa, and the reflux ratio is 0.02 to 1.
7. Process according to claim 6, characterized in that the ethylene separation column is a tray column or a packed column, preferably a packed column.
8. The method of claim 4, wherein the recycle ethylene compressor has a compression ratio of 1.2 to 3.
9. The method of claim 8, wherein the recycle ethylene compressor is a positive displacement compressor or a centrifugal compressor.
10. The process of claim 1, wherein the ethylene splitter bottoms liquid stream is returned to the propanal reactor.
11. An apparatus for use in the method of any one of claims 1 to 10, comprising: the system comprises a propionaldehyde reactor (101), an ethylene separation tower (102) connected with the propionaldehyde reactor (101) through a pipeline, a propionaldehyde cooler (103) connected with the ethylene separation tower (102) through a pipeline, a propionaldehyde after-cooler (104) connected with the propionaldehyde cooler (103) through a pipeline, a circulating ethylene compressor (105) respectively connected with the propionaldehyde after-cooler (104) and the propionaldehyde reactor (101) through pipelines, an ethylene separation tower reflux tank (106), an ethylene separation tower reflux pump (107) and a stripping tower (108);
the ethylene separation tower reflux tank (106) is respectively connected with the propionaldehyde cooler (103), the propionaldehyde after-cooler (104) and the ethylene separation tower reflux pump (107) through pipelines;
the ethylene separation column reflux pump (107) is connected with the ethylene separation column (102) and the stripping column (108) through pipelines respectively;
the stripper column (108) is connected to the propanal reactor (101) by a line.
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| CN102115433A (en) * | 2010-12-06 | 2011-07-06 | 淄博诺奥化工有限公司 | Synthesis method of propionaldehyde by low-pressure carbonyl of ethylene |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102115433A (en) * | 2010-12-06 | 2011-07-06 | 淄博诺奥化工有限公司 | Synthesis method of propionaldehyde by low-pressure carbonyl of ethylene |
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Application publication date: 20210813 |