CN220676803U - Process unit for producing ethylene and by-product vinyl acetate at low temperature - Google Patents
Process unit for producing ethylene and by-product vinyl acetate at low temperature Download PDFInfo
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- CN220676803U CN220676803U CN202322222174.XU CN202322222174U CN220676803U CN 220676803 U CN220676803 U CN 220676803U CN 202322222174 U CN202322222174 U CN 202322222174U CN 220676803 U CN220676803 U CN 220676803U
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- Prior art keywords
- vinyl acetate
- gas
- ethane
- ethylene
- pipeline
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- XTXRWKRVRITETP-UHFFFAOYSA-N Vinyl acetate Chemical compound CC(=O)OC=C XTXRWKRVRITETP-UHFFFAOYSA-N 0.000 title claims abstract description 57
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 239000005977 Ethylene Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000006227 byproduct Substances 0.000 title claims abstract description 16
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims abstract description 75
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 57
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 claims abstract description 28
- 238000002360 preparation method Methods 0.000 claims abstract description 25
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 239000000047 product Substances 0.000 claims abstract description 16
- 239000000463 material Substances 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 42
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 30
- 239000001301 oxygen Substances 0.000 claims description 30
- 229910052760 oxygen Inorganic materials 0.000 claims description 30
- 239000011261 inert gas Substances 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- 125000000896 monocarboxylic acid group Chemical group 0.000 abstract description 2
- 230000008878 coupling Effects 0.000 abstract 1
- 238000010168 coupling process Methods 0.000 abstract 1
- 238000005859 coupling reaction Methods 0.000 abstract 1
- 239000000126 substance Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004227 thermal cracking Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 229920002972 Acrylic fiber Polymers 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- YBCVMFKXIKNREZ-UHFFFAOYSA-N acoh acetic acid Chemical compound CC(O)=O.CC(O)=O YBCVMFKXIKNREZ-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a process device for producing ethylene and byproduct vinyl acetate at low temperature, which comprises an ethane oxidative dehydrogenation device, a device for preparing vinyl acetate from ethylene and acetic acid, gas-liquid separation equipment, a vinyl acetate rectifying device and an ethylene rectifying tower which are sequentially connected along the direction of main material flow. Oxidative dehydrogenation unit C by coupling ethane 2 H 6 +0.5O 2 →C 2 H 4 +H 2 O and vinyl acetate preparation device C 2 H 4 +CH 3 COOH+0.5O 2 →C 2 H 3 OOCCH 3 +H 2 O realizes that ethane is used as a raw material to be dehydrogenated to generate ethylene and vinyl acetate under a mild reaction condition, improves the richness of ethane oxidative dehydrogenation products and improves the adaptability of the process to the market.
Description
Technical Field
The utility model relates to a process device for producing ethylene and vinyl acetate as a byproduct at low temperature, which is suitable for producing ethylene in the chemical industry and belongs to the field of petrochemical industry.
Background
Ethylene (C) 2 H 4 ) Is one of chemical products with the largest yield in the world, is an important chemical basic raw material, and is mainly used for chemical products such as synthetic fibers, rubber, plastics, acrylic fibers, adhesives and the like. Ethylene products currently account for over 40% of organic chemicals, while about 75% of petrochemical products are produced from ethylene, which is an important place in national economy. Ethylene production scale, technology and yield have been worldwide one of the important markers for the measurement of the state petrochemical industry development.
In recent years, along with the innovation of North America shale gas, ethane is taken as a raw material, the cost for preparing ethylene through a thermal cracking path is greatly reduced, and a plurality of low-carbon alkane cracking devices are established in China. However, ethane thermal cracking is an endothermic reaction, limited by thermodynamic equilibrium, and the reaction temperature is higher than 900 ℃ to cause high energy consumption, so that the cracking furnace is easy to coke, the device equipment is complex, and the operation cost is high. In comparison, the Oxidative Dehydrogenation (ODHE) of ethane is a potential alternative process, and can effectively overcome the problems of equilibrium conversion rate, carbon deposition and the like while reducing the reaction temperature due to the exothermic property. However, the generation of acetic acid (acetic acid) is accompanied in the ODHE process, and the traditional method is to carry out alkali washing separation, so that the utilization rate of raw materials is relatively low, and the separation cost is relatively high.
Disclosure of Invention
The object of the present utility model is to solve the above problemsSolves the problem of utilizing acetic acid as a byproduct in the prior ethane oxidative dehydrogenation process, and designs a process device which passes through an ethane oxidative dehydrogenation device C 2 H 6 +0.5O 2 →C 2 H 4 +H 2 O (thermocatalysis) and vinyl acetate preparation device C using ethylene and acetic acid as raw materials 2 H 4 +CH 3 COOH+0.5O 2 →C 2 H 3 OOCCH 3 +H 2 O is used for dehydrogenation under mild reaction conditions by taking ethane as a raw material to generate ethylene and vinyl acetate.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a process device for producing ethylene and by-product vinyl acetate at low temperature comprises an ethane oxidative dehydrogenation device, a vinyl acetate preparation device, gas-liquid separation equipment, a vinyl acetate rectifying tower and an ethylene rectifying tower which are sequentially connected along the direction of main material flow; the product gas outlet of the ethane oxidative dehydrogenation device is connected with the gas inlet end of the vinyl acetate preparation device, the product gas outlet of the vinyl acetate preparation device is connected with the gas-liquid separation equipment, the liquid phase outlet of the gas-liquid separation equipment is connected with the vinyl acetate rectifying tower, and the gas phase outlet of the gas-liquid separation equipment is connected with the ethylene rectifying tower.
Further, the air inlet end of the ethane oxidative dehydrogenation device is provided with first air mixing equipment, and three air inlet branch pipes are respectively arranged on the first air mixing equipment and are respectively an oxygen branch pipe, an ethane branch pipe and an inert gas branch pipe.
Further, an oxygen pipeline and an acetic acid steam pipeline are respectively arranged at the air inlet end of the vinyl acetate preparation device, the oxygen pipeline is connected with an oxygen branch pipe through a three-way valve, and an oxygen control valve and an acetic acid control valve are respectively arranged on the oxygen pipeline and the acetic acid steam pipeline.
Furthermore, a second air mixing device is arranged at the air inlet end of the vinyl acetate preparation device, and the oxygen pipeline and the acetic acid steam pipeline are respectively connected with the air inlet end of the second air mixing device.
Further, the system also comprises a deethanizer, wherein the gas phase separated by the gas-liquid separation equipment sequentially enters the ethylene rectifying tower and the deethanizer, an ethane gas outlet of the deethanizer is connected with the ethane branch pipe through an ethane pipeline, and an ethane control valve is arranged on the ethane pipeline.
Further, the gas-liquid separation equipment comprises a condenser and a gas-liquid separator which are sequentially connected with the vinyl acetate preparation device.
Compared with the prior art, the utility model has the following advantages:
the utility model couples ethane oxidative dehydrogenation reaction and reaction of preparing vinyl acetate from ethylene and acetic acid, increases the utilization of byproduct acetic acid, improves the product richness prepared by ethane oxidative dehydrogenation process, improves the market adaptability of the process, greatly reduces the energy consumption of preparing ethylene by ethane thermal cracking at present, greatly improves the utilization rate of raw materials, reduces the production equipment of products and greatly improves the economical efficiency of process routes compared with the conventional ethane oxidative dehydrogenation process. Can realize the preparation of ethylene and vinyl acetate by low-energy consumption and high-efficiency ethane oxidation.
Drawings
FIG. 1 is a schematic diagram of a process unit for producing ethylene by-product vinyl acetate at low temperature.
In the figure: 1. an ethane oxidative dehydrogenation unit; 2. a vinyl acetate production device; 3. a gas-liquid separator; 4. vinyl acetate rectifying tower; 5. an ethylene rectifying tower; 6. a deethanizer; 7. a first gas mixing device; 8. a second gas mixing device; 9. a condenser; 10. a gas-liquid separator; 101. an oxygen manifold; 102. an ethane branch; 103. an inert gas manifold; 11. an oxygen pipe; 12. an oxygen control valve; 13. acetic acid steam pipeline; 14. an acetic acid control valve; 15. an ethane pipeline; 16. ethane control valve.
Detailed Description
The following describes specific embodiments of the present utility model in detail with reference to the drawings. It should be understood that the detailed description and specific examples, while indicating and illustrating the utility model, are not intended to limit the utility model.
As shown in figure 1, a process device for producing ethylene by-product vinyl acetate at low temperature comprises an ethane oxidative dehydrogenation device 1, a vinyl acetate preparation device 2, gas-liquid separation equipment 3, a vinyl acetate rectifying tower 4 and an ethylene rectifying tower 5 which are sequentially connected along the direction of main material flow; the product gas outlet of the ethane oxidative dehydrogenation device 1 is connected with the gas inlet end of the vinyl acetate preparation device 2, the product gas outlet of the vinyl acetate preparation device 2 is connected with the gas-liquid separation device 3, the liquid phase outlet of the gas-liquid separation device 3 is connected with the vinyl acetate rectifying tower 4, and the gas phase outlet of the gas-liquid separation device 3 is connected with the ethylene rectifying tower 5.
The device generates partial vinyl acetate by reacting ethylene and acetic acid (or introducing acetic acid externally) generated in ethane oxidative dehydrogenation reaction, the liquid after gas-liquid separation enters a vinyl acetate rectifying device to obtain polymerization-grade vinyl acetate, and the ethylene in the gas is used as a main product to be separated and collected by an ethylene rectifying tower.
As shown in fig. 1, in one embodiment of the present utility model:
the gas inlet end of the ethane oxidative dehydrogenation device 1 is provided with a first gas mixing device 7, and three gas inlet branch pipes, namely an oxygen branch pipe 101, an ethane branch pipe 102 and an inert gas branch pipe 103, are respectively arranged on the first gas mixing device 7.
The first gas mixing device 7 is used for receiving and mixing ethane, oxygen and inert gas (such as nitrogen) from three gas inlet branch pipes, mixing and preheating raw material gas, and then delivering the raw material gas to the ethane oxidative dehydrogenation device 1.
In one embodiment:
the air inlet end of the vinyl acetate preparation device 2 is respectively provided with an oxygen pipeline 11 and an acetic acid steam pipeline 13, the oxygen pipeline 11 is connected with an oxygen branch pipe 101 through a three-way valve, and the oxygen pipeline 11 and the acetic acid steam pipeline 13 are respectively provided with an oxygen control valve 12 and an acetic acid control valve 14.
The acetic acid and oxygen inlets of the vinyl acetate preparation device are independently connected through a pipeline, and a control valve is arranged on the pipeline.
In a preferred scheme, a second gas mixing device 8 is further arranged at the air inlet end of the vinyl acetate preparation device 2, and the oxygen pipeline 11 and the acetic acid steam pipeline 13 are respectively connected with the air inlet end of the second gas mixing device 8.
The product gas after the ethane oxidative dehydrogenation reaction enters into the second gas mixing equipment 8, the waste heat of the product gas of the ethane oxidative dehydrogenation device 1 is utilized to preheat the acetic acid and the oxygen which independently enter into the second gas mixing equipment 8, and the mixed gas after the preheating enters into the vinyl acetate preparation device 2 again, so that the heat energy is effectively utilized, and the cost is saved.
In another embodiment of the utility model, the process device for producing the ethylene by-product vinyl acetate comprises an ethane oxidative dehydrogenation device 1, a vinyl acetate preparation device 2, a gas-liquid separation device 3, a vinyl acetate rectifying tower 4 and an ethylene rectifying tower 5 which are sequentially connected along the direction of the main material flow, and further comprises a deethanizer 6, wherein the gas phase separated by the gas-liquid separation device 3 sequentially enters the ethylene rectifying tower 5 and the deethanizer 6, an ethane gas outlet of the deethanizer 6 is connected with the ethane branch pipe 102 through an ethane pipeline 15, and an ethane control valve 16 is arranged on the ethane pipeline 15.
After being treated by the deethanizer 6, the incompletely reacted ethane is returned to the ethane branch 102 through an ethane pipeline 15 and enters the first gas mixing device 7 to be mixed and preheated with oxygen and inert gas.
Further, the gas-liquid separation equipment comprises a condenser and a gas-liquid separator which are sequentially connected with the vinyl acetate preparation device.
In one embodiment:
specifically, as shown in fig. 1, the gas-liquid separation apparatus includes a condenser 9 and a gas-liquid separator 10 connected in this order to the vinyl acetate production device 2.
Specifically, in this embodiment, as shown in fig. 1, the tail gas from the gas outlet of the ethane oxidative dehydrogenation device, the acetic acid vapor in the acetic acid vapor pipeline and the oxygen in the oxygen pipeline are mixed, and the residual heat from the tail gas from the ethane oxidative dehydrogenation device is used to preheat and mix the reaction gas, and the mixed reaction gas enters the gas inlet of the vinyl acetate preparation device.
The foregoing has shown and described the basic principles, principal features and advantages of the utility model. It will be understood by those skilled in the art that the present utility model is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present utility model, and various changes and modifications may be made therein without departing from the spirit and scope of the utility model, which is defined by the appended claims. The scope of the utility model is defined by the appended claims and equivalents thereof.
Claims (6)
1. The process device for producing the ethylene byproduct vinyl acetate at low temperature is characterized by comprising an ethane oxidative dehydrogenation device, a vinyl acetate preparation device, gas-liquid separation equipment, a vinyl acetate rectifying tower and an ethylene rectifying tower which are sequentially connected along the direction of a main material flow;
the product gas outlet of the ethane oxidative dehydrogenation device is connected with the gas inlet end of the vinyl acetate preparation device, the product gas outlet of the vinyl acetate preparation device is connected with the gas-liquid separation equipment, the liquid phase outlet of the gas-liquid separation equipment is connected with the vinyl acetate rectifying tower, and the gas phase outlet of the gas-liquid separation equipment is connected with the ethylene rectifying tower.
2. The process device for producing ethylene by-product vinyl acetate at low temperature according to claim 1, wherein the air inlet end of the ethane oxidative dehydrogenation device is provided with a first air mixing device, and three air inlet branch pipes are respectively arranged on the first air mixing device, namely an oxygen branch pipe, an ethane branch pipe and an inert gas branch pipe.
3. The process device for producing ethylene by-product vinyl acetate at low temperature according to claim 2, wherein an oxygen pipeline and an acetic acid steam pipeline are respectively arranged at the air inlet end of the vinyl acetate preparation device, the oxygen pipeline is connected with an oxygen branch pipe through a three-way valve, and an oxygen control valve and an acetic acid control valve are respectively arranged on the oxygen pipeline and the acetic acid steam pipeline.
4. A process unit for producing ethylene by-product vinyl acetate at low temperature according to claim 3, wherein a second air mixing device is further arranged at the air inlet end of the vinyl acetate preparation unit, and the oxygen pipeline and the acetic acid steam pipeline are respectively connected with the air inlet end of the second air mixing device.
5. The process unit for producing ethylene by-product vinyl acetate at low temperature according to claim 2, further comprising a deethanizer, wherein the gas phase separated by the gas-liquid separation device sequentially enters the ethylene rectifying tower and the deethanizer, an ethane gas outlet of the deethanizer is connected with the ethane branch pipe through an ethane pipeline, and an ethane control valve is arranged on the ethane pipeline.
6. The process device for producing ethylene by-product vinyl acetate at low temperature according to claim 1, wherein the gas-liquid separation equipment comprises a condenser and a gas-liquid separator which are sequentially connected with the vinyl acetate preparation device.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322222174.XU CN220676803U (en) | 2023-08-18 | 2023-08-18 | Process unit for producing ethylene and by-product vinyl acetate at low temperature |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322222174.XU CN220676803U (en) | 2023-08-18 | 2023-08-18 | Process unit for producing ethylene and by-product vinyl acetate at low temperature |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220676803U true CN220676803U (en) | 2024-03-29 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322222174.XU Active CN220676803U (en) | 2023-08-18 | 2023-08-18 | Process unit for producing ethylene and by-product vinyl acetate at low temperature |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220676803U (en) |
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2023
- 2023-08-18 CN CN202322222174.XU patent/CN220676803U/en active Active
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