CN111217665B - Fine separation device and separation method for olefin catalytic cracking product - Google Patents
Fine separation device and separation method for olefin catalytic cracking product Download PDFInfo
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- CN111217665B CN111217665B CN202010249817.8A CN202010249817A CN111217665B CN 111217665 B CN111217665 B CN 111217665B CN 202010249817 A CN202010249817 A CN 202010249817A CN 111217665 B CN111217665 B CN 111217665B
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- 238000000926 separation method Methods 0.000 title claims abstract description 54
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 22
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 21
- VLKZOEOYAKHREP-UHFFFAOYSA-N hexane Substances CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims abstract description 154
- 239000007788 liquid Substances 0.000 claims abstract description 49
- 238000010992 reflux Methods 0.000 claims abstract description 40
- 238000001816 cooling Methods 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims description 36
- 239000007791 liquid phase Substances 0.000 claims description 34
- 239000012071 phase Substances 0.000 claims description 34
- 238000007599 discharging Methods 0.000 claims description 8
- 238000005086 pumping Methods 0.000 claims description 8
- 238000000034 method Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000005191 phase separation Methods 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 8
- 239000000126 substance Substances 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 25
- 239000007789 gas Substances 0.000 description 16
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 11
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 239000006227 byproduct Substances 0.000 description 7
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- 239000013064 chemical raw material Substances 0.000 description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 3
- 239000001273 butane Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 150000005673 monoalkenes Chemical class 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 239000003254 gasoline additive Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 150000003738 xylenes Chemical class 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a fine separation device and a separation method for olefin catalytic cracking products, which belong to the field of chemical technology, wherein the separation device comprises a de-hexane device arranged between a depropanizer and a debutanizer, the de-hexane device comprises a reboiler, a de-hexane tower kettle liquid cooling device, a de-hexane tower condenser, a de-hexane tower reflux tank and a reflux pump which are mutually communicated through pipelines; the fine separation device can realize the device and the separation method for finely separating the C4-C6+ components, the conversion of the economic added value of the product from low to high is completed, and the high economic added value utilization of the C6+ product is facilitated.
Description
Technical Field
The invention relates to the field of chemical technology, in particular to a fine separation device and a separation method for an olefin catalytic cracking product.
Background
Aromatic hydrocarbons are an important basic raw material for producing large amounts of petrochemical products in the world today, and polymers produced from aromatic hydrocarbons play an important role in modern life. At present, the main products of global aromatic hydrocarbon are light aromatic hydrocarbon such as benzene, toluene, xylene and the like; aromatic hydrocarbons are an important base stock for the petrochemical industry, accounting for about 30% of the total number of about 800 ten thousand known compounds, with BTX aromatics (benzene, toluene, xylenes) being referred to as primary basic organic feedstock. The aromatic hydrocarbon resource can be used for extending and developing a plurality of series product chains, and the application of the aromatic hydrocarbon resource is expanded to the fields of synthetic resin, paint, fuel, medicine and the like.
The olefin catalyst cracking process byproducts of C4 and above C5 fractions, the C5 above fractions on the market at present are mainly used as industrial and civil fuels and gasoline additives, and along with the continuous rising of crude oil prices in recent years, the economy of the downstream use of the resources is questionable; aromatic hydrocarbon is used as an important organic chemical raw material, the economic additional value is higher, in the existing olefin catalytic cracking technology, the fraction above C5 contains aromatic hydrocarbon components, but the purity is not high, the standard of the organic chemical raw material cannot be met, the market value of the aromatic hydrocarbon cannot be effectively reflected, and the fine separation technology aiming at the fraction above C5 is not available in the prior art, so that the equipment capable of finely separating C4-C6+ products (crude mixed benzene) in byproducts of an olefin catalytic cracking technology is needed to be designed, aromatic hydrocarbon meeting the standard of the organic chemical raw material is further obtained, the conversion of the economic additional value of the product from low to high is finished, and the market and economic benefits are improved.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a device and a method for finely separating C4-C6+ components in an olefin catalytic cracking product so as to realize high economic additional value utilization of the C6+ product.
In order to solve the problems, the invention provides the following technical scheme: the utility model provides a catalytic cracking product fine separation device of olefin, includes the separation system, and the difference with prior art lies in that this application adds the device of taking off hexane between the depropanizer and the debutanizer in prior art separation system, takes off the hexane device and includes taking off the hexane tower, takes off the hexane tower and includes feed inlet, top of tower gaseous phase export, tower cauldron discharge gate, top of tower return port, removes reboiler mouth, reboiler return port, level gauge mouth, thermometer mouth, overhead relief valve; the liquid level meter port is used for measuring the liquid level in the hexane removing tower, the thermometer port is used for setting the temperature and measuring the temperature of each point in the tower, and the tower top safety valve is a relief system, so that the safety of the air pressure in the tower is ensured.
The bottom of the hexane removal tower is connected with a reboiler, the reboiler is a tube shell Cheng Xingshi, a tube side medium is a hexane removal tower kettle liquid, a shell side medium is steam, and the two mediums are heat-conducting but not contacted; the discharging end of the depropanizer is communicated with the feeding port of the dehexanizer, the discharging port of the tower kettle is sequentially communicated with a liquid pump of the dehexanizer kettle and liquid cooling equipment of the dehexanizer kettle through pipelines, and the discharging end of the liquid cooling equipment of the dehexanizer kettle is communicated with a product tank;
the gas phase outlet of the tower top is communicated with a hexane removal tower condenser, the discharge end of the hexane removal tower condenser is communicated with a hexane removal tower reflux tank, the hexane removal tower reflux tank is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet is communicated with the upstream of an OCC device (the OCC technology is a process for preparing propylene and ethylene by further catalytic cracking of mono-olefins in byproduct C4 and C5 of an MTO device), the liquid phase outlet is communicated with a reflux pump, the discharge end of the reflux pump is provided with a pipeline I and a pipeline II, the pipeline II is communicated with the feed end of the debutanizer, and the pipeline I is communicated with the reflux port of the tower top.
It should be noted that, the effect of the de-hexane tower of this application is that the gas-liquid separation of tower inner kettle material is realized through the distillation, and the required C6+ product of this application is discharged through tower cauldron discharge gate, and gaseous C4-C5 is discharged through top of the tower gas phase export, and the gas phase kettle material circulation backward flow after the de-hexane tower reflux tank can realize liquefaction, and then distill through the de-hexane tower again to improve C6+ rate of separation, the de-butane tower is as the low reaches device of de-hexane tower.
In order to effectively control the air pressure, the liquid level and the like in the tower, the technical scheme of the invention further comprises that a flow valve is arranged at a tower kettle discharge hole and a pipeline II of the hexane removal tower.
In order to improve the heat exchange effect of the heat source of the dehexane tower, the technical scheme of the invention further comprises that the reboiler is a vertical thermosiphon reboiler, the reboiler is provided with a low-pressure steam inlet and a steam outlet, the steam outlet is communicated with a dehexane tower steam condensate tank, the dehexane tower steam condensate tank is used for cooling steam discharged from the steam outlet of the reboiler, and the dehexane tower steam condensate tank is provided with a steam condensate outlet.
In order to improve the cooling effect of the de-hexane tower kettle liquid, the technical scheme of the invention further comprises that the de-hexane tower kettle liquid cooling equipment comprises a de-hexane tower kettle liquid cooler and a de-hexane tower kettle liquid aftercooler which are communicated sequentially through pipelines.
Preferably, the technical scheme of the invention further comprises that the de-hexane tower condenser is provided with a circulating water cooling device.
The second object of the invention is to provide a separation method of a fine separation device for olefin catalytic cracking products, comprising the following steps:
(1) The mixed kettle liquid containing C4-C6 and C6+ at the discharge end of the depropanizer enters the depropanizer from the feed inlet of the depropanizer, the temperature in the depropanizer gradually rises under the action of a reboiler, gas phase and liquid phase separation is realized, C4-C6 is changed into a gas phase kettle material, and C6+ is changed into a liquid phase kettle material;
(2) Discharging the liquid phase kettle material in the step (1) from a tower kettle discharge port, pumping the liquid phase kettle material to a de-hexane tower kettle liquid cooling device for cooling after the liquid phase kettle material is boosted by a de-hexane tower kettle liquid pump, and then conveying the liquid phase kettle material to a C6+ product tank;
(3) The gas phase kettle material (C4-C6) in the step (1) is discharged through a gas phase outlet at the top of the tower, is cooled through a de-hexane tower condenser, enters a de-hexane tower reflux tank for gas-liquid separation, is discharged through a gas phase outlet of the de-hexane tower reflux tank and enters a downstream OCC device as a reaction raw material, and is discharged through a liquid phase outlet and enters a reflux pump;
(4) The reflux pump is boosted, one part of the liquid phase material in the step (3) is pumped to a reflux port at the top of the tower through a pipeline I and enters the de-hexane tower for reflux recycling, and the other part of the liquid phase material is pumped to the debutanizer as a feed through a pipeline II to separate C4.
Preferably, the technical scheme of the invention further comprises that the internal tower top pressure of the de-hexane tower is 0.3MPaG; the condenser of the de-hexane tower is cooled by circulating water, and the condensing temperature is 52.3 ℃; the pumping pressure of the reflux pump is 0.64MpaG; pumping pressure of a liquid pump of the de-hexane tower kettle is 0.79MPaG; the temperature of the product of cooling C6+ is 40 ℃ by cooling equipment in the bottom of the de-hexane tower, and the high-efficiency and high-quality operation of the device can be realized by the de-hexane tower separation device controlled by the parameters.
The technical scheme of the invention also comprises that the flow of the discharge hole of the tower kettle and the liquid level of the de-hexane tower kettle are controlled by a flow valve positioned at the discharge hole of the tower kettle; the pressure at the top of the tower and the flow at the gas phase outlet of the top of the hexane removing tower are controlled by a flow valve at the gas phase outlet of a reflux tank of the hexane removing tower; the flow of the pipeline II and the liquid level in the reflux tank of the de-hexane tower are controlled by a flow valve positioned in the pipeline II, and the temperature in the de-hexane tower is controlled by a heat source steam inlet regulating valve positioned in the reboiler.
Further, the technical scheme of the invention also comprises that liquid phase kettle materials discharged by a liquid pump of the tower kettle are conveyed to a C6 < + > product tank after being sequentially subjected to two-stage cooling of a liquid cooler of the de-hexane tower kettle and a post-cooler of the de-hexane tower kettle.
The beneficial effects of the invention are as follows: compared with the prior art, the invention aims to provide a separation device and a separation method for finely separating C6+ from crude butane and mixed fractions above C5 which are byproducts in the process of preparing propylene and ethylene (OCC technology) by olefin catalytic pyrolysis, so as to realize high value-added utilization of C6+, and realize the technical effects as follows:
firstly, the separation system in the prior art is modified, a de-hexane tower device is added between a de-propanizer and a debutanizer to realize fine separation of byproducts of OCC technology, the kettle materials at the discharge end of the de-propanizer are distilled and separated through the de-hexane tower, the liquid-phase C6+ liquid-phase kettle materials are discharged through a discharge hole of the kettle and cooled to obtain C6+ products, C4-C6 is discharged from a gas-phase outlet at the top of the tower as a gas phase, and separation of C6+ and C4-C6 is realized;
secondly, after the gas-phase kettle material is sequentially processed by a hexane removal tower condenser and a reflux tank, the gas-phase material enters a downstream OCC device, one part of the liquid-phase material enters a debutanizer for C4 separation, and the other part of the liquid-phase material flows back to the hexane removal tower for secondary separation, so that the separation effect of C6+ can be effectively improved;
finally, through the hexane-removing tower separating device, separation of C4, C5-C6 and C6+ in the byproducts of the process for preparing propylene and ethylene by catalytic cracking of olefin is realized, fine separation of C6+ is realized, and the conversion of the economic added value of the product from low to high is completed.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are required to be used in the description of the embodiments or the prior art will be briefly described below, and it will be obvious to those skilled in the art that other drawings can be obtained from these drawings without inventive effort.
FIG. 1 is a schematic structural diagram of a fine separation device for an olefin catalytic cracking product in an embodiment.
Wherein, 1 is a depropanizer, 2 is a dehexanizer, 3 is a feed inlet of the dehexanizer, 4 is a reboiler, 5 is a reboiler return inlet, 6 is a flow valve, 7 is a dehexanizer inlet, 8 is a dehexanizer steam condensate tank, 9 is a dehexanizer kettle liquid pump, 10 is a dehexanizer kettle liquid cooler, 11 is a dehexanizer kettle liquid aftercooler, 12 is a product tank, 13 is a kettle discharge port, 14 is a tower top gas phase outlet, 15 is a dehexanizer condenser, 16 is a dehexanizer reflux tank, 17 is an OCC device, 18 is a reflux pump, 19 is a pipeline I, 20 is a tower top reflux port, 21 is a pipeline II, 22 is a debutanizer, 23 is a liquid level meter port, 24 is a thermometer port, and 25 is a tower top safety valve.
Detailed Description
In order to make the technical solution of the present invention better understood by those skilled in the art, the technical solution of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are only some embodiments of the present invention, not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present invention without making any inventive effort, shall fall within the scope of the present invention.
In the description of the present invention, it should be understood that the terms "center," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like indicate orientations or positional relationships based on the orientation or positional relationships shown in the drawings, merely to simplify the description of the present invention, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
As can be seen from the accompanying drawings, a separation method of a fine separation device for olefin catalytic cracking products comprises the following steps:
(1) The mixed kettle liquid containing C4-C6 and C6+ at the discharge end of the depropanizer 1 enters a depropanizer 2 from a feeding port 3 of the depropanizer, the temperature in the depropanizer 2 is gradually increased under the action of a reboiler 4, the pressure at the top of the interior of the depropanizer 2 is 0.3MPaG, gas phase and liquid phase separation is realized, the gas phase kettle material is mainly C4-C6, and the liquid phase kettle material is C6+; wherein, the reboiler 4 is vertical thermosiphon type, the heat source adopts 1.0MPaG low pressure steam, the de-hexane tower is provided with a reboiler return port 5 and a de-reboiler port 7, the heat exchange between the de-hexane tower kettle liquid and the steam realizes the heating function of the reboiler, and the reboiler 4 is communicated with a de-hexane tower steam condensate tank 8;
(2) The liquid phase kettle material in the step (1) is discharged from a kettle discharge hole 13, is boosted to 0.79MPaG by a de-hexane kettle liquid pump 9, sequentially passes through a de-hexane kettle liquid cooler 10 and a de-hexane kettle liquid aftercooler 11 for two-stage cooling, is cooled to 40 ℃ and then is conveyed to a C6 < + > product tank 12; the flow of the tower kettle discharge port 13 and the liquid level of the de-hexane tower kettle are controlled by a flow valve positioned at the tower kettle discharge port 13;
(3) After being discharged from a gas-phase kettle material (C4-C6) in the step (1) through a gas-phase outlet 14 at the top of the tower, the gas-phase kettle material is firstly cooled by circulating cooling water through a hexane removal tower condenser 15, the condensation temperature is 52.3 ℃, then enters a hexane removal tower reflux tank 16 for gas-liquid separation, a gas-phase material (mostly C4-C6 mono-olefin) is discharged from a gas-phase outlet of the hexane removal tower reflux tank 16 and enters the upstream of an OCC device 17 as a reaction raw material, a flow valve 6 is arranged at the gas-phase outlet, and a liquid-phase material is discharged from a liquid-phase outlet and enters a reflux pump 18;
(4) The reflux pump 18 is boosted to 0.64MpaG, and part of the liquid phase material in the step (3) is pumped to the tower top reflux port 20 through a pipeline I19 and enters the de-hexane tower 2 for reflux recycling, the other part is pumped to the debutanizer tower 22 through a pipeline II 21 as a feed for C4 separation, and the flow rate of the pipeline II 21 and the liquid level in the de-hexane tower reflux tank 16 are controlled through a flow valve 6 positioned in the pipeline II 21.
In addition, the de-hexane tower is also provided with a liquid level meter port 23, a thermometer port 24 and a tower top safety valve 25.
According to the olefin catalytic cracking product fine separation device, through the separation method, separation of C4, C5-C6 and C6+ of OCC technical byproducts is achieved, fine separation of C6+ is further achieved, conversion of low-to-high economic added value of the product is achieved, and high economic added value utilization of the C6+ product is facilitated.
Although the present invention has been described in detail by way of preferred embodiments with reference to the accompanying drawings, the present invention is not limited thereto. Various equivalent modifications and substitutions may be made in the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and it is intended that all such modifications and substitutions be within the scope of the present invention/be within the scope of the present invention as defined by the appended claims. Therefore, the protection scope of the present invention shall be subject to the protection scope of the claims.
Claims (7)
1. An olefin catalytic cracking product fine separation device, includes a separation system, characterized in that: a hexane removing device is added between a depropanizer and a debutanizer in a separation system, the hexane removing device comprises a hexane removing tower, the hexane removing tower comprises a feed inlet, a tower top gas phase outlet, a tower bottom discharge outlet, a tower top return port, a reboiler removing port, a reboiler return port, a liquid level meter port, a thermometer port and a tower top safety valve; the bottom of the hexane removal tower is connected with a reboiler; the reboiler is a vertical thermosiphon type reboiler, the reboiler is provided with a low-pressure steam inlet and a steam outlet, the steam outlet is communicated with a hexane removal tower steam condensate tank, and the hexane removal tower steam condensate tank is provided with a steam condensate outlet; the reboiler is a tube shell Cheng Xingshi, the tube side medium is the bottom liquid of the hexane removal tower, the tube side medium is steam, and the two mediums are heat-conducting but not contacted; the discharging end of the depropanizer is communicated with the feeding port of the dehexanizer, the discharging port of the tower kettle is sequentially communicated with a liquid pump of the dehexanizer, a liquid cooler of the dehexanizer kettle and a aftercooler of the dehexanizer kettle through pipelines, and the discharging end of the aftercooler of the dehexanizer kettle is communicated with a product tank; the gas phase outlet of the tower top is communicated with a hexane removal tower condenser, the discharge end of the hexane removal tower condenser is communicated with a hexane removal tower reflux tank, the hexane removal tower reflux tank is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet is communicated with the upstream of an OCC device, the liquid phase outlet is communicated with a reflux pump, the discharge end of the reflux pump is provided with a pipeline I and a pipeline II, the pipeline II is communicated with the feed end of the debutanizer, and the pipeline I is communicated with the tower top reflux port.
2. The olefin catalytic cracking product fine separation device according to claim 1, characterized in that: and a discharge hole of the tower kettle of the hexane removal tower and a pipeline II are provided with flow valves.
3. The olefin catalytic cracking product fine separation device according to claim 1, characterized in that: the condenser of the de-hexane tower is provided with a circulating water cooling device.
4. A separation method suitable for the fine separation device of olefin catalytic cracking products as claimed in claim 1, characterized in that: the method comprises the following steps:
(1) The mixed kettle liquid containing C4-C6 and C6+ at the discharge end of the depropanizer enters the depropanizer from the feed inlet of the depropanizer, the temperature in the depropanizer gradually rises under the action of a reboiler, gas phase and liquid phase separation is realized, C4-C6 is changed into a gas phase kettle material, and C6+ is changed into a liquid phase kettle material;
(2) Discharging the liquid phase kettle material in the step (1) from a tower kettle discharge port, pumping the liquid phase kettle material to a de-hexane tower kettle liquid cooling device for cooling after the liquid phase kettle material is boosted by a tower kettle liquid pump, and then conveying the liquid phase kettle material to a C6+ product tank;
(3) The gas phase kettle material in the step (1) is discharged through a gas phase outlet at the top of the tower, is cooled through a condenser of the de-hexane tower, enters a reflux tank of the de-hexane tower for gas-liquid separation, is discharged through a gas phase outlet of the reflux tank of the de-hexane tower, enters the upstream of an OCC device as a reaction raw material, and is discharged through a liquid phase outlet and enters a reflux pump;
(4) And (3) pumping a part of the liquid phase material in the step (3) to a top reflux port through a pipeline I and entering a de-hexane tower for reflux recycling, and pumping the other part of the liquid phase material to the debutanizer as a feed through a pipeline II.
5. The separation method of the fine separation device for olefin catalytic cracking products according to claim 4, wherein: the internal tower top pressure of the de-hexane tower is 0.3MPaG; the condenser of the de-hexane tower is cooled by circulating water, and the condensing temperature is 52.3 ℃; the pumping pressure of the reflux pump is 0.64MpaG; pumping pressure of a liquid pump of the de-hexane tower kettle is 0.79MPaG; cooling the product with cooling equipment in the de-hexane tower kettle to 40 ℃.
6. The separation method of the fine separation device for olefin catalytic cracking products according to claim 4, wherein: the flow of the discharge port of the tower kettle and the liquid level of the de-hexane tower kettle are controlled through a flow valve positioned at the discharge port of the tower kettle; the flow of the pipeline II and the liquid level in the reflux tank of the hexane removal tower are controlled through a flow valve positioned in the pipeline II.
7. The separation method of the fine separation device for olefin catalytic cracking products according to claim 4, wherein: and (2) conveying the liquid phase kettle materials discharged by the liquid pump of the tower kettle in the step (2) to a C6 < + > product tank after sequentially passing through a liquid cooler of the de-hexane tower kettle and a two-stage cooling device of the liquid post-hexane tower kettle.
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| CN202010249817.8A CN111217665B (en) | 2020-04-01 | 2020-04-01 | Fine separation device and separation method for olefin catalytic cracking product |
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| CN202010249817.8A CN111217665B (en) | 2020-04-01 | 2020-04-01 | Fine separation device and separation method for olefin catalytic cracking product |
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| CN111217665B true CN111217665B (en) | 2024-01-19 |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1653020A (en) * | 2002-07-19 | 2005-08-10 | 乐吉股份公司 | Method for producing propylene from a flow containing C4 to C8 olefins |
| CN1962579A (en) * | 2005-11-11 | 2007-05-16 | 中国石油化工股份有限公司 | Method for separating carbon-containing olefin cracked product |
| CN212025224U (en) * | 2020-04-01 | 2020-11-27 | 联泓新材料科技股份有限公司 | Fine separation device for olefin catalytic cracking products |
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2020
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1653020A (en) * | 2002-07-19 | 2005-08-10 | 乐吉股份公司 | Method for producing propylene from a flow containing C4 to C8 olefins |
| CN1962579A (en) * | 2005-11-11 | 2007-05-16 | 中国石油化工股份有限公司 | Method for separating carbon-containing olefin cracked product |
| CN212025224U (en) * | 2020-04-01 | 2020-11-27 | 联泓新材料科技股份有限公司 | Fine separation device for olefin catalytic cracking products |
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