CN220564513U - Process unit for producing ethylene byproduct synthesis gas at low temperature - Google Patents
Process unit for producing ethylene byproduct synthesis gas at low temperature Download PDFInfo
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- CN220564513U CN220564513U CN202322222173.5U CN202322222173U CN220564513U CN 220564513 U CN220564513 U CN 220564513U CN 202322222173 U CN202322222173 U CN 202322222173U CN 220564513 U CN220564513 U CN 220564513U
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- gas
- ethane
- ethylene
- synthesis gas
- low temperature
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 239000005977 Ethylene Substances 0.000 title claims abstract description 54
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 32
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 23
- 239000006227 byproduct Substances 0.000 title claims abstract description 17
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 66
- 238000000926 separation method Methods 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 28
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 claims abstract description 24
- 238000002407 reforming Methods 0.000 claims abstract description 23
- 239000000047 product Substances 0.000 claims abstract description 17
- 239000000463 material Substances 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 74
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 28
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 14
- 239000001569 carbon dioxide Substances 0.000 claims description 14
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000011261 inert gas Substances 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 238000006356 dehydrogenation reaction Methods 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000002994 raw material Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 3
- 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
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 229920002972 Acrylic fiber Polymers 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000008021 deposition Effects 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
- 239000000203 mixture Substances 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
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 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
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a process device for producing ethylene byproduct synthesis gas at low temperature, which comprises a main reactorThe material flow direction is sequentially connected with an ethane oxidative dehydrogenation device, a gas-liquid separation device, an ethylene rectifying tower, an ethane dry reforming device and a synthesis gas separation device; the product gas outlet of the ethane oxidative dehydrogenation device is connected with gas-liquid separation equipment, the product gas outlet of the gas-liquid separation equipment is connected with an ethylene rectifying tower, the tail gas outlet of the ethylene rectifying tower is connected with the gas inlet end of an ethane dry reforming device, and the gas outlet of the ethane dry reforming device is connected with the gas inlet of the synthesis gas separation equipment. By oxidative dehydrogenation of ethane unit C 2 H 6 +0.5O 2 →C 2 H 4 +H 2 O and ethane dry reformer 2CO 2 +C 2 H 6 →3H 2 +4CO, while simplifying the apparatus, allows dehydrogenation of ethane as a feedstock to ethylene and synthesis gas.
Description
Technical Field
The utility model relates to a process device for producing ethylene by-product synthesis gas 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. The byproduct COx of the ODHE process, along with unreacted ethane, will increase the separation costs of the plant, making the oxidative dehydrogenation process route of ethane a certain economic disadvantage.
Disclosure of Invention
In view of the above, the present utility modelIn order to reduce the problem of higher separation cost in the current ethane oxidative dehydrogenation process, a process device is designed, and an ethane oxidative dehydrogenation device C is used for separating the ethane 2 H 6 +0.5O 2 →C 2 H 4 +H 2 O and ethane dry reformer 2CO 2 +C 2 H 6 →3H 2 +4CO, while simplifying the apparatus, allows dehydrogenation of ethane as a feedstock to ethylene and synthesis gas.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a process device for producing ethylene byproduct synthesis gas at low temperature comprises an ethane oxidative dehydrogenation device, gas-liquid separation equipment, an ethylene rectifying tower, an ethane dry reforming device and synthesis gas separation equipment which are sequentially connected along the direction of main material flow; the product gas outlet of the ethane oxidative dehydrogenation device is connected with gas-liquid separation equipment, the product gas outlet of the gas-liquid separation equipment is connected with an ethylene rectifying tower, the tail gas outlet of the ethylene rectifying tower is connected with the gas inlet end of an ethane dry reforming device, and the gas outlet of the ethane dry reforming device is connected with the gas inlet of the synthesis gas separation equipment.
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, the air inlet end of the ethane dry reforming device is also provided with a carbon dioxide pipeline, and the carbon dioxide pipeline is provided with a control valve.
Furthermore, the air inlet end of the ethane dry reforming device is also provided with a second air mixing device, and the air inlet of the second air mixing device is respectively connected with a carbon dioxide pipeline and the tail gas outlet of the ethylene rectifying tower.
And the tail gas directly from the ethylene rectifying tower and the downstream carbon dioxide are mixed in second gas mixing equipment and then enter an ethane dry reforming device, so that an ethane removal process is not needed.
Further, a product gas outlet of the ethylene rectifying tower is connected with an ethylene storage tank.
Further, the synthesis gas separation device comprises a second gas-liquid separation device, a deethanizer and a decarbonator which are connected in sequence.
Further, the gas-liquid separation device or the second liquid separation device comprises a condenser and a gas-liquid separator which are connected in sequence.
Compared with the prior art, the utility model has the following advantages:
the process device greatly reduces the energy consumption for preparing ethylene by ethane thermal cracking at present, greatly improves the economical efficiency of a process route compared with a conventional ethane oxidative dehydrogenation process device, and can reduce carbon emission while realizing low-energy consumption and high-efficiency ethane oxidation for preparing ethylene and synthesis gas.
Drawings
FIG. 1 is a schematic diagram of a process unit for producing ethylene byproduct synthesis gas at low temperature;
FIG. 2 is a schematic diagram of a synthesis gas separation apparatus according to the present utility model.
In the figure: 1. an ethane oxidative dehydrogenation unit; 2. a gas-liquid separator; 3. an ethylene rectifying tower; 4. an ethane dry reformer; 5. a synthesis gas separation device; 6. a first gas mixing device; 7. a second gas mixing device; 8. a condenser; 9. a gas-liquid separator; 10. an ethylene storage tank; 11. a carbon dioxide pipeline; 12. a control valve; 13. a second liquid separation device; 14. a deethanizer; 15. a decarbonation tower; 101. an oxygen manifold; 102. an ethane branch; 103. inert gas branch pipe.
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.
A process device for producing ethylene by-product synthesis gas at low temperature comprises an ethane oxidative dehydrogenation device 1, a gas-liquid separation device 2, an ethylene rectifying tower 3, an ethane dry reforming device 4 and a synthesis gas separation device 5 which are sequentially connected along the direction of a main material flow; the product gas outlet of the ethane oxidative dehydrogenation device 1 is connected with the gas-liquid separation equipment 2, the product gas outlet of the gas-liquid separation equipment 2 is connected with the ethylene rectifying tower 3, the tail gas outlet of the ethylene rectifying tower 3 is connected with the gas inlet end of the ethane dry reforming device 4, and the gas outlet of the ethane dry reforming device 4 is connected with the gas inlet of the synthesis gas separation equipment 5.
As shown in FIG. 1, the device is characterized in that ethane and oxygen are subjected to oxidative dehydrogenation reaction of ethane to generate ethylene and other byproducts and unreacted ethane, and the ethylene is separated and collected as a main product through an ethylene rectifying tower; and the tail gas of the ethylene rectifying tower enters an ethane dry reforming device to be used as a raw material for reaction, and the obtained reaction tail gas enters a synthetic gas separation device 5 to obtain synthetic gas with a certain carbon monoxide and hydrogen ratio.
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 6, 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 6.
The first gas mixing device 6 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 this embodiment, the air inlet end of the ethane dry reforming device 4 is further provided with a carbon dioxide pipeline 11, and a control valve 12 is arranged on the carbon dioxide pipeline 11.
Specifically, the tail gas of the ethane oxidative dehydrogenation device 1 enters an ethylene rectifying tower 3 through a product separated by the gas-liquid separation device 2, and an air outlet of the ethylene rectifying tower 3 is connected and mixed with a carbon dioxide pipeline 11 and then is connected to an ethane dry reforming device 4.
As shown in fig. 1, in one embodiment of the present utility model:
the air inlet end of the ethane dry reforming device 4 is also provided with a second air mixing device 7, and the air inlet of the second air mixing device 7 is respectively connected with a carbon dioxide pipeline 11 and the tail gas outlet of the ethylene rectifying tower 3.
The carbon dioxide and unreacted ethane and byproducts which are independently fed into the second gas mixing equipment 7 are mixed and preheated, and the preheated mixed gas is fed into the ethane dry reforming device 4 for reaction to obtain synthesis gas.
As shown in fig. 1, in one embodiment of the present utility model: the product gas outlet of the ethylene rectifying tower 3 is connected with an ethylene storage tank 10.
In one embodiment of the utility model:
the synthesis gas separation device comprises a second gas-liquid separation device 13, a deethanizer 14 and a decarbonator 15 which are connected in sequence. As shown in fig. 2, the gas after the reaction in the ethane dry reforming device 4 is separated by a gas-liquid separation device, and the separated gas sequentially enters a deethanizer 14 and a decarbonator 15 to remove the ethane and carbon dioxide which are not completely reacted in the gas, and finally the synthesis gas of the mixture of carbon monoxide and hydrogen is obtained.
As shown in fig. 1, in one embodiment of the present utility model: the gas-liquid separation equipment 2 comprises a condenser 8 and a gas-liquid separator 9 which are sequentially connected with the ethane oxidative dehydrogenation 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 (7)
1. The process device for producing the ethylene byproduct synthesis gas at low temperature is characterized by comprising an ethane oxidative dehydrogenation device, gas-liquid separation equipment, an ethylene rectifying tower, an ethane dry reforming device and synthesis gas separation equipment 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 gas-liquid separation equipment, the product gas outlet of the gas-liquid separation equipment is connected with an ethylene rectifying tower, the tail gas outlet of the ethylene rectifying tower is connected with the gas inlet end of an ethane dry reforming device, and the gas outlet of the ethane dry reforming device is connected with the gas inlet of the synthesis gas separation equipment.
2. The process device for producing ethylene byproduct synthesis gas 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 unit for producing ethylene byproduct synthesis gas at low temperature according to claim 1, wherein the air inlet end of the ethane dry reforming unit is further provided with a carbon dioxide pipeline, and a control valve is arranged on the carbon dioxide pipeline.
4. A process unit for producing ethylene byproduct synthesis gas at low temperature according to claim 3, wherein the air inlet end of the ethane dry reforming unit is further provided with a second air mixing device, and the air inlet of the second air mixing device is respectively connected with a carbon dioxide pipeline and the tail gas outlet of the ethylene rectifying tower.
5. The process unit for producing ethylene byproduct synthesis gas at low temperature according to claim 1, wherein a product gas outlet of the ethylene rectifying tower is connected with an ethylene storage tank.
6. The process unit for producing ethylene byproduct synthesis gas at low temperature according to claim 1, wherein the synthesis gas separation device comprises a second gas-liquid separation device, a deethanizer and a decarbonation tower which are connected in sequence.
7. A process unit for the low temperature production of ethylene by-product synthesis gas according to claim 1 or 6, wherein the gas-liquid separation device or the second liquid separation device comprises a condenser and a gas-liquid separator connected in sequence.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322222173.5U CN220564513U (en) | 2023-08-18 | 2023-08-18 | Process unit for producing ethylene byproduct synthesis gas at low temperature |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322222173.5U CN220564513U (en) | 2023-08-18 | 2023-08-18 | Process unit for producing ethylene byproduct synthesis gas at low temperature |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220564513U true CN220564513U (en) | 2024-03-08 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322222173.5U Active CN220564513U (en) | 2023-08-18 | 2023-08-18 | Process unit for producing ethylene byproduct synthesis gas at low temperature |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220564513U (en) |
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2023
- 2023-08-18 CN CN202322222173.5U patent/CN220564513U/en active Active
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