CN210765167U - Oxide stripping unit of MTO device capable of removing heavy oil hydrocarbon - Google Patents
Oxide stripping unit of MTO device capable of removing heavy oil hydrocarbon Download PDFInfo
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- CN210765167U CN210765167U CN201921489324.0U CN201921489324U CN210765167U CN 210765167 U CN210765167 U CN 210765167U CN 201921489324 U CN201921489324 U CN 201921489324U CN 210765167 U CN210765167 U CN 210765167U
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Abstract
The utility model discloses a MTO device can remove oxide strip unit of heavy hydrocarbon, it includes quench tower, knockout tower, oxide strip tower, product gas knockout drum, dimethyl ether strip tower, oxide absorption tower, wash column, skimming jar and heavy hydrocarbon jar, the export passes through the pipeline intercommunication with the feed inlet of skimming jar at the bottom of the tower of product gas knockout drum, the bottom discharge mouth of skimming jar passes through the pipeline intercommunication with the feed inlet of oxide strip tower, the overflow mouth of skimming jar and the feed inlet intercommunication of heavy hydrocarbon jar. The utility model discloses a set up the skimming jar, can effectively get rid of the heavy hydrocarbon in the oxide strip unit, avoid its enrichment and influence the heat transfer effect of heat exchanger, the separation effect of tower cauldron and the quality of water of technology in whole strip unit, avoided causing the technology undulant because of quality of water exceeds standard, guaranteed the normal steady operation of strip unit.
Description
The technical field is as follows:
the utility model relates to an MTO device can remove oxide strip unit of heavy oil hydrocarbon belongs to coal chemical industry field.
Background art:
the methanol-to-olefin (MTO) process refers to a chemical process technology for producing low-carbon olefins by using coal-based or natural gas-based synthesized methanol as a raw material and by means of a fluidized bed reaction form similar to a catalytic cracking device. The main product of the process for preparing olefin from methanol is ethylene (C)2H4) Propylene (C)3H6). The MTO device consists of a methanol-to-olefin part and an olefin separation part, wherein the methanol-to-olefin part comprises a reaction regeneration unit, a thermal unit, a quenching unit and an oxide stripping unit; the olefin separation part comprises a feed gas compression unit, an acid gas removal unit, an alkali washing unit, a gas phase and liquid phase drying and drying bed regeneration unit, a propane removal unit, a demethanization unit, an ethane removal unit, an ethylene rectification unit, a propylene rectification unit, a butane removal unit, a propylene refrigeration unit and the like; wherein the oxide stripping unit is that the product gas obtained from the reaction regeneration unit is cooled by a quench tower to remove a part of water, and the product gas is produced at about 120 DEG CAnd (3) feeding product gas (comprising ethylene, propylene, methane, ethane, water vapor, C4, C5, acetone, acetaldehyde, methanol, dimethyl ether and the like) into a separation tower, further cooling to about 42 ℃ for water removal, and discharging the condensed water vapor from the bottom of the separation tower. After the components containing ethylene, propylene, methane, ethane, C4, C5, acetone, acetaldehyde, methanol and dimethyl ether at the top of the separation tower are separated by a product gas-liquid separation tank, liquid phases (C4, C5, acetone, acetaldehyde, methanol and dimethyl ether) are pumped into an oxide stripping tower to strip oxides (C4, C5, acetone, acetaldehyde, methanol and dimethyl ether) so as to separate the oxides from water; the gas phase obtained from the product gas separation tank is fed into the liquid separation tank through a dimethyl ether stripping tower to be separated, so that light condensed oil and a gas phase containing ethylene and propylene are obtained, the light condensed oil enters a water washing tower and is washed by methanol and water, useful components dimethyl ether and methanol in the light condensed oil are recovered, and the light condensed oil returns to an oxide stripping tower to extract oxides; the washed stripped component containing C4 and C5 is sent to a subsequent system for separation and debutanization; feeding the gas phase containing ethylene and propylene obtained by the feeding liquid separation tank of the dimethyl ether stripping tower into an oxide absorption tower, mixing and washing the gas phase with the water phase fed from the oxide stripping tower after stripping, dissolving the oxide in the ethylene and the propylene in water, and feeding the mixture into the oxide stripping tower again for washing; after the oxide stripping tower is stripped, the oxide is sent into the reactor to react again, and raw materials or intermediate products in the oxide stripping tower are utilized; however, due to the process parameters of the separation tower, condensed water is discharged from the bottom, light gas is discharged from the upper part, heavy hydrocarbon mostly stays in the middle of the tower, so that a tower plate is wrapped by heavy oil, and the separation effect is influenced; moreover, the bottom water of the product gas separation tank and the bottom water of the water washing tower contain certain heavy hydrocarbon, the heavy hydrocarbon is sent into the oxide stripping tower for steam stripping and enters the reactor, and the heavy hydrocarbon does not participate in the reaction, is only enriched in the whole unit and stays in the heat exchanger, so that the heat exchange effect is influenced; stay in the tower kettle to influence the separation effect; the waste water is carried in washing water and water produced at the bottom of a stripping tower, the water quality of process water is influenced, COD of the process water exceeds the standard, and process fluctuation is caused.
The utility model has the following contents:
the utility model aims to provide an MTO device can remove the oxide stripping unit of heavy oil hydrocarbon.
The utility model discloses by following technical scheme implement: an oxide stripping unit of an MTO device capable of removing heavy oil hydrocarbon comprises a quench tower, a separation tower, an oxide stripping tower, a product gas separation tank, a dimethyl ether stripping tower, an oxide absorption tower and a water washing tower,
the feed inlet of the quenching tower is communicated with the product gas outlet of the reactor through a pipeline, the top outlet of the quenching tower is communicated with the feed inlet of the separation tower through a pipeline, the bottom outlet of the separation tower is communicated with the feed inlet of the quenching tower through a pipeline, the top outlet of the separation tower is communicated with the feed inlet of the product gas separation tank through a pipeline, the top outlet of the product gas separation tank is communicated with the feed inlet of the dimethyl ether stripping tower through a pipeline, the top outlet of the dimethyl ether stripping tower is communicated with the feed inlet of the oxide absorption tower through a pipeline, and the bottom outlet of the dimethyl ether stripping tower is communicated with the feed inlet of the water washing tower through a pipeline; the bottom outlet of the product gas separation tank, the bottom outlet of the oxide absorption tower and the bottom outlet of the water washing tower are communicated with the feed inlet of the oxide stripping tower through pipelines, the bottom discharge port of the oxide stripping tower is communicated with the feed inlet of the oxide absorption tower through a pipeline, and the top discharge port of the oxide stripping tower is communicated with the feed inlet of the reactor through a pipeline; it still includes skimming jar and heavy hydrocarbon jar, the export at the bottom of the tower of product gas knockout drum with the feed inlet of skimming jar passes through the pipeline intercommunication, the bottom discharge mouth of skimming jar with the feed inlet of oxide stripper passes through the pipeline intercommunication, the overflow mouth of skimming jar with the feed inlet intercommunication of heavy hydrocarbon jar.
The skimming tank is a standing tank body, and a feed inlet is formed in the tank body, so that heavy components and light components are layered. Set up the heavy ends export bottom jar body, set up the overflow mouth at jar body lateral part, because heavy hydrocarbon is less for aqueous solution density in this scheme, lie in jar body upper portion behind the layering, so discharge from the overflow mouth.
The device further comprises a water pump and a heat exchanger, wherein a feed inlet of the water pump is communicated with a discharge outlet in the middle of the separation tower through a pipeline, and a discharge outlet of the water pump is communicated with a hot medium outlet of the heat exchanger through a pipeline; the pipeline communicated between the water pump and the heat exchanger is also communicated with a feed inlet of the oil skimming tank through an oil skimming pipe, and the oil skimming pipe is provided with an oil skimming valve.
The utility model has the advantages that: the utility model discloses a set up the skimming jar, can effectively get rid of the heavy hydrocarbon in the oxide strip unit, avoid its enrichment and influence the heat transfer effect of heat exchanger, the separation effect of tower cauldron and the quality of water of technology in whole strip unit, avoided causing the technology undulant because of quality of water exceeds standard, guaranteed the normal steady operation of strip unit.
Description of the drawings:
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 description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
Fig. 1 is a schematic system diagram of the present embodiment.
Wherein: the device comprises a reactor 1, a quench tower 2, a separation tower 3, an oxide stripping tower 4, a product gas separation tank 5, a dimethyl ether stripping tower 6, an oxide absorption tower 7, a water washing tower 8, an oil skimming tank 9, a heavy hydrocarbon tank 10, a water pump 11, a heat exchanger 12, an oil skimming pipe 13 and an oil skimming valve 14.
The specific implementation mode is as follows:
the technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
An oxide stripping unit of an MTO device capable of removing heavy oil hydrocarbon comprises a quench tower 2, a separation tower 3, an oxide stripping tower 4, a product gas separation tank 5, a dimethyl ether stripping tower 6 and an oxide absorption tower 7, the device comprises a water scrubber 8, a skimming tank 9, a heavy hydrocarbon tank 10, a water pump 11 and a heat exchanger 12, wherein a feed inlet of a quench tower 2 is communicated with a product gas outlet of a reactor 1 through a pipeline, a tower top outlet of the quench tower 2 is communicated with a feed inlet of a separation tower 3 through a pipeline, a tower bottom outlet of the separation tower 3 is communicated with a feed inlet of the quench tower 2 through a pipeline, a tower top outlet of the separation tower 3 is communicated with a feed inlet of a product gas separation tank 5 through a pipeline, a tank top outlet of the product gas separation tank 5 is communicated with a feed inlet of a dimethyl ether stripping tower 6 through a pipeline, a tower top outlet of the dimethyl ether stripping tower 6 is communicated with a feed inlet of an oxide absorption tower 7 through a pipeline, and a tower bottom outlet of the; the outlet at the bottom of the product gas separation tank 5, the outlet at the bottom of the oxide absorption tower 7 and the outlet at the bottom of the water washing tower 8 are all communicated with the feed inlet of the oxide stripping tower 4 through pipelines, the discharge outlet at the bottom of the oxide stripping tower 4 is communicated with the feed inlet of the oxide absorption tower 7 through a pipeline, and the discharge outlet at the top of the oxide stripping tower 4 is communicated with the feed inlet of the reactor 1 through a pipeline; the outlet at the bottom of the tower of product gas knockout drum 5 passes through the pipeline intercommunication with the feed inlet of skimming jar 9, and the bottom discharge gate of skimming jar 9 passes through the pipeline intercommunication with the feed inlet of oxide stripper 4, and the overflow mouth of skimming jar 9 communicates with the feed inlet of heavy hydrocarbon jar 10. A feed inlet of the water pump 11 is communicated with a discharge outlet in the middle of the separation tower 3 through a pipeline, and a discharge outlet of the water pump 11 is communicated with a heat medium outlet of the heat exchanger 12 through a pipeline; the pipeline between the water pump 11 and the heat exchanger 12 is also communicated with the feed inlet of the oil skimming tank 9 through an oil skimming pipe 13, and the oil skimming pipe 13 is provided with an oil skimming valve 14.
The working principle is as follows:
the product gas obtained from the reactor 1 is cooled in a quench tower 2, then a part of water is removed, the product gas (comprising ethylene, propylene, methane, ethane, water vapor, C4, C5, acetone, acetaldehyde, methanol, dimethyl ether and the like) with the temperature of about 120 ℃ is obtained at the top of the quench tower 2, the product gas enters a separation tower 3 for further cooling and dewatering, the product gas at the top of the separation tower 3 is cooled to about 42 ℃, and the water vapor is condensed and then discharged from the bottom of the separation tower 3. After the components containing ethylene, propylene, methane, ethane, C4, C5, acetone, acetaldehyde, methanol and dimethyl ether at the top of the separation tower 3 are separated by a product gas-liquid separation tank 5, the gas phase obtained by the product gas-liquid separation tank 5 enters a dimethyl ether stripping tower 6 for stripping operation to obtain light condensed oil and a gas phase containing ethylene and propylene, the gas phase containing ethylene and propylene obtained by the dimethyl ether stripping tower 6 enters an oxide absorption tower 7 and is mixed and washed with the water phase sent after being stripped by the oxide stripping tower 4, and oxides in the ethylene and the propylene are dissolved in water and are sent to the oxide stripping tower 4 again for stripping; the light condensed oil obtained from the dimethyl ether stripping tower 6 enters a water washing tower 8 to be washed by methanol and water, useful components dimethyl ether and methanol in the light condensed oil are recovered and returned to the oxide stripping tower 4 to extract oxides; the washed components containing C4 and C5 are sent to a subsequent system for separation and debutanization; the liquid phase obtained by the oxide absorption tower 7 and the liquid phase obtained by the water washing tower 8 are both sent into the oxide stripping tower 4 for stripping operation; the liquid phase obtained by the product gas-liquid separation tank 5 contains heavy hydrocarbon and is firstly sent into the oil skimming tank 9, and the heavy hydrocarbon is firstly layered due to the different density of the heavy hydrocarbon and other liquids, floats on the upper part of the oil skimming tank 9 and is discharged from an overflow port on the upper part of the oil skimming tank 9; the rest liquid phase is sent into an oxide stripping tower 4 for stripping operation; in addition, in order to better realize the stripping effect, the water pump 11 and the heat exchanger 12 are used for heating the material in the middle of the separation tower 3, and heavy hydrocarbon in the separation tower 3 is concentrated in the material in the middle, so that the oil skimming valve 14 can be opened during heating, part of the heated material flows back to the separation tower 3, the stripping effect is optimized, the other part of the heated material enters the oil skimming tank 9, and the heated material is subjected to stripping operation in the oxide stripping tower 4 after heavy oil is skimmed; after the material in the oxide stripping tower 4 is stripped, the oxide is sent into the reactor 1 for reaction again, and the raw material or intermediate product in the oxide stripping tower is utilized; due to the fact that the oil skimming tank 9 is arranged, heavy hydrocarbon in the system is skimmed in the oil skimming tank 9, circulation in the system is avoided, and the phenomenon that the heat exchange effect and the separation effect are affected due to adhesion in a heat exchanger and a separation tower is avoided; and the phenomenon that the process water is carried in washing water and the bottom produced water of a stripping tower to influence the water quality of the process water, so that the COD of the process water exceeds the standard and the process fluctuation is caused is avoided.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (2)
1. An oxide stripping unit of an MTO device capable of removing heavy oil hydrocarbon comprises a quench tower, a separation tower, an oxide stripping tower, a product gas separation tank, a dimethyl ether stripping tower, an oxide absorption tower and a water washing tower, the feed inlet of the quenching tower is communicated with the product gas outlet of the reactor through a pipeline, the outlet at the top of the quenching tower is communicated with the feed inlet of the separation tower through a pipeline, the outlet at the bottom of the separation tower is communicated with the feed inlet of the quenching tower through a pipeline, the outlet at the top of the separation tower is communicated with the feed inlet of the product gas separation tank through a pipeline, the tank top outlet of the product gas separation tank is communicated with the feed inlet of the dimethyl ether stripping tower through a pipeline, the outlet of the dimethyl ether stripping tower is communicated with the feed inlet of the oxide absorption tower through a pipeline, the outlet of the bottom of the dimethyl ether stripping tower is communicated with the feed inlet of the water washing tower through a pipeline; the bottom outlet of the product gas separation tank, the bottom outlet of the oxide absorption tower and the bottom outlet of the water washing tower are communicated with the feed inlet of the oxide stripping tower through pipelines, the bottom discharge port of the oxide stripping tower is communicated with the feed inlet of the oxide absorption tower through a pipeline, and the top discharge port of the oxide stripping tower is communicated with the feed inlet of the reactor through a pipeline;
its characterized in that, it still includes skimming jar and heavy hydrocarbon jar, the export at the bottom of the tower of product gas knockout drum with the feed inlet of skimming jar passes through the pipeline intercommunication, the bottom discharge mouth of skimming jar with the feed inlet of oxide stripper passes through the pipeline intercommunication, the overflow mouth of skimming jar with the feed inlet intercommunication of heavy hydrocarbon jar.
2. The MTO device oxide stripping unit capable of removing heavy oil hydrocarbon according to claim 1, characterized by further comprising a water pump and a heat exchanger, wherein a feed inlet of the water pump is communicated with a middle discharge outlet of the separation tower through a pipeline, and a discharge outlet of the water pump is communicated with a heat medium outlet of the heat exchanger through a pipeline; the pipeline communicated between the water pump and the heat exchanger is also communicated with a feed inlet of the oil skimming tank through an oil skimming pipe, and the oil skimming pipe is provided with an oil skimming valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921489324.0U CN210765167U (en) | 2019-09-09 | 2019-09-09 | Oxide stripping unit of MTO device capable of removing heavy oil hydrocarbon |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921489324.0U CN210765167U (en) | 2019-09-09 | 2019-09-09 | Oxide stripping unit of MTO device capable of removing heavy oil hydrocarbon |
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| Publication Number | Publication Date |
|---|---|
| CN210765167U true CN210765167U (en) | 2020-06-16 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201921489324.0U Active CN210765167U (en) | 2019-09-09 | 2019-09-09 | Oxide stripping unit of MTO device capable of removing heavy oil hydrocarbon |
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| CN (1) | CN210765167U (en) |
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