CN111217665A - 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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- CN111217665A CN111217665A CN202010249817.8A CN202010249817A CN111217665A CN 111217665 A CN111217665 A CN 111217665A CN 202010249817 A CN202010249817 A CN 202010249817A CN 111217665 A CN111217665 A CN 111217665A
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- 238000000926 separation method Methods 0.000 title claims abstract description 58
- 150000001336 alkenes Chemical class 0.000 title claims abstract description 25
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 25
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 title claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 53
- 238000010992 reflux Methods 0.000 claims abstract description 41
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims abstract description 21
- 238000001816 cooling Methods 0.000 claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 7
- 239000000463 material Substances 0.000 claims description 42
- 239000012071 phase Substances 0.000 claims description 36
- 239000007791 liquid phase Substances 0.000 claims description 35
- 238000005086 pumping Methods 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000011144 upstream manufacturing Methods 0.000 claims description 3
- 239000000047 product Substances 0.000 abstract description 28
- 239000006227 byproduct Substances 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000001311 chemical methods and process Methods 0.000 abstract description 2
- 230000002349 favourable effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 26
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 9
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000013064 chemical raw material Substances 0.000 description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 3
- 239000005977 Ethylene Substances 0.000 description 3
- 150000005673 monoalkenes Chemical class 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
- 238000006467 substitution reaction Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 2
- 239000007792 gaseous phase Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 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
- 239000001273 butane Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001276 controlling effect 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
- 239000003814 drug Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002816 fuel additive 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
- 238000002360 preparation method Methods 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
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- 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 an olefin catalytic cracking product, belonging to the field of chemical processes, wherein the separation device comprises a hexane removal device arranged between a depropanizer and a debutanizer, the hexane removal device comprises a reboiler, a dehexanizer kettle liquid cooling device, a dehexanizer condenser, a dehexanizer reflux tank and a reflux pump which are mutually communicated through pipelines, the invention also discloses a separation method applicable to the fine separation device, and the fine separation of C6+ in an olefin catalytic cracking byproduct in the OCC technology can be realized; the fine separation device and the separation method can realize fine separation of components from C4 to C6+, complete conversion of the economic added value of the product from low to high, and are favorable for realizing high economic added value utilization of the C6+ product.
Description
Technical Field
The invention relates to the field of chemical processes, in particular to a fine separation device and a separation method for an olefin catalytic cracking product.
Background
Aromatic hydrocarbons are important basic raw materials for producing a large number of petrochemical products in the world at present, and polymers produced by using the 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; aromatics are important base feedstocks for the petrochemical industry, accounting for about 30% of the total of about 800 million known compounds, with BTX aromatics (benzene, toluene, xylenes) being referred to as primary base organic feedstocks. Aromatic hydrocarbon resources can be used for extending and developing a plurality of series product chains, and the application of the aromatic hydrocarbon resources is extended to the fields of synthetic resin, paint, fuel, medicine and the like.
The cracking process of the olefin catalyst produces C4 and C5 fractions as byproducts, the C5 fractions on the market are mainly used as industrial and civil fuel and gasoline additives, and the economy of the downstream application of the resources is questionable with the rising of the price of crude oil in recent years; aromatic hydrocarbon is used as an important organic chemical raw material, the economic added value is high, 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 organic chemical raw material cannot be effectively embodied, and a fine separation technology aiming at the fraction above C5 is not available in the prior art, so that an urgent need exists for designing equipment capable of finely separating C4-C6 + products (crude mixed benzene) in byproducts of the olefin catalytic cracking process, and further obtaining the aromatic hydrocarbon meeting the standard of the organic chemical raw material, so that the conversion of the economic added value of the product from low to high is completed, 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 separation method for finely separating C4-C6 + components in an olefin catalytic cracking product so as to realize high economic value-added utilization of a C6+ product.
In order to solve the problems, the invention provides the following technical scheme: a kind of olefin catalytic cracking products fine separation device, including the separation system, different from prior art lie in, this application increases the dehexanizer between depropanizer and debutanizer in the separation system of prior art, the dehexanizer includes the dehexanizer, the dehexanizer includes feed inlet, gas phase outlet of the top of the tower, discharge port of the column kettle, reflux port of the top of the tower, remove reboiler port, reboiler return port, level gauge port, thermometer port, top of the tower relief valve; the liquid level meter port is used for measuring the liquid level in the dehexadecane tower, the thermometer port is used for setting the temperature and measuring the temperature of each point in the tower, and the safety valve at the top of the tower is a discharge system to ensure the safety of the air pressure in the tower.
The bottom of the dehexanizer is connected with a reboiler, the reboiler is in a tube pass form, a tube pass medium is the dehexanizer kettle liquid, a shell pass medium is steam, and the two media have heat conduction but are not in contact with each other; the discharge end of the depropanizing tower is communicated with the feed inlet of the depropanizing tower, the discharge port of the tower kettle is sequentially communicated with a depropanizing tower kettle liquid pump and a depropanizing tower kettle liquid cooling device through a pipeline, and the discharge end of the depropanizing tower kettle liquid cooling device is communicated with a product tank;
the top of the tower is communicated with a dehexanizer condenser, the discharge end of the dehexanizer condenser is communicated with a dehexanizer reflux tank, the dehexanizer 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 used for further catalytic cracking of mono-olefin in MTO device by-products C4 and C5 to prepare propylene and ethylene), 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 debutaner, and the pipeline I is communicated with the top of the tower reflux port.
It should be noted that the effect of the dehexanizer of this application is that the gas-liquid separation of cauldron material in the tower is realized through the distillation, and the required C6+ product of this application is discharged through tower cauldron discharge gate, and gaseous C4-C5 are discharged through the gaseous phase export in top of the tower, and the gaseous phase cauldron material circulation reflux after the dehexanizer reflux tank can realize liquefying, and then distills through the dehexanizer once more to improve C6+ separation rate, the debutanizer is as the low reaches device of dehexanizer.
In order to effectively control the air pressure, the liquid level and the like in the tower, the technical scheme of the invention also comprises that a tower kettle discharge port and a pipeline II of the dehexanizer are provided with flow valves.
In order to improve the heat exchange effect of the heat source of the dehexanizer, the technical scheme of the invention also comprises that the reboiler is a vertical thermosyphon reboiler, the reboiler is provided with a low-pressure steam inlet and a steam outlet, the steam outlet is communicated with the dehexanizer steam condensate tank, the dehexanizer steam condensate tank is used for cooling the steam discharged from the steam outlet of the reboiler, and the dehexanizer steam condensate tank is provided with a steam condensate outlet.
In order to improve the cooling effect of the dehexanizer kettle liquid, the technical scheme of the invention also comprises that the dehexanizer kettle liquid cooling equipment comprises a dehexanizer kettle liquid cooler and a dehexanizer kettle liquid aftercooler which are sequentially communicated through a pipeline.
Preferably, the technical scheme of the invention also comprises that the condenser of the dehexanizer is provided with a circulating water cooling device.
The invention also aims to provide a separation method of a fine separation device for an olefin catalytic cracking product, which comprises the following steps:
(1) the mixed kettle liquid containing C4-C6 and C6+ at the discharge end of the depropanizing tower enters the depropanizing tower from a feed inlet of the depropanizing tower, the temperature in the depropanizing tower is gradually increased under the action of a reboiler to realize the separation of gas phase and liquid phase, C4-C6 is changed into gas phase kettle material, and C6+ is changed into liquid phase kettle material;
(2) discharging the liquid phase kettle material in the step (1) from a discharge hole of the tower kettle, boosting the pressure by a de-hexane tower kettle liquid pump, pumping the liquid phase kettle material to de-hexane tower kettle liquid cooling equipment for cooling, and then conveying the liquid phase kettle material to a product tank of C6 +;
(3) after the gas phase kettle materials (C4-C6) in the step (1) are discharged from a gas phase outlet at the top of the tower, the gas phase kettle materials are firstly cooled by a condenser of a de-hexane tower and then enter a reflux tank of the de-hexane tower for gas-liquid separation, the gas phase materials (mostly C4-C6 mono-olefin) are discharged from a gas phase outlet of the reflux tank of the de-hexane tower and enter a downstream OCC device as reaction raw materials, and the liquid phase materials are discharged from a liquid phase outlet and enter a reflux pump;
(4) and (3) pumping a part of the liquid-phase material in the step (3) to a reflux port at the top of the tower through a pipeline I by the aid of a reflux pump for reflux recirculation, and pumping the other part of the liquid-phase material to a debutanizer through a pipeline II for feeding so as to separate C4.
Preferably, the technical scheme of the invention also comprises that the internal tower top pressure of the dehexanizer is 0.3 MPaG; a condenser of the dehexanizer is cooled by circulating water, and the condensation temperature is 52.3 ℃; the pumping pressure of the reflux pump is 0.64 MpaG; the pumping pressure of the dehexanizer bottoms pump is 0.79 MPaG; the temperature of C6+ products is cooled by the dehexanizer kettle liquid cooling equipment to be 40 ℃, and the efficient and high-quality operation of the device can be realized by the dehexanizer 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 dehexanizer 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 inside the dehexanizer and the flow of the gas phase outlet at the top of the tower are controlled by a flow valve positioned at the gas phase outlet of a reflux tank of the dehexanizer; the flow of the pipeline II and the liquid level in the reflux tank of the dehexanizer are controlled by a flow valve positioned on the pipeline II, and the temperature in the dehexanizer is controlled by a regulating valve positioned on a heat source steam inlet of a reboiler.
Further, the technical scheme of the invention also comprises that the liquid phase kettle material discharged by the tower kettle liquid pump is sequentially cooled by a dehexanizer kettle liquid cooler and a dehexanizer kettle liquid aftercooler in two stages and then is conveyed to a product tank of C6 +.
The invention has the beneficial effects that: 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 C5-above fraction which are byproducts in the process of preparing propylene and ethylene by catalytic cracking of olefin (OCC technology), so as to realize high value-added utilization of C6+, and in order to realize the technical effects:
firstly, the separation system in the prior art is improved, a dehexanizer device is additionally arranged between a depropanizer and a debutanizer, so that the fine separation of OCC technical byproducts is realized, the distillation separation is carried out on kettle materials at the discharge end of the depropanizer through the dehexanizer, C6+ liquid phase kettle materials of a liquid phase are discharged through a discharge port of a tower kettle and cooled to obtain a C6+ product, C4-C6 become a gas phase and are discharged from a gas phase outlet at the top of the tower, so that the separation of C6+ and C4-C6 is realized;
secondly, after the gas phase kettle material is sequentially treated by a condenser and a reflux tank of the dehexanizer, the gas phase material enters a downstream OCC device, one part of the liquid phase material enters the debutaner to be subjected to C4 separation, and the other part of the liquid phase material reflows to the dehexanizer to be subjected to secondary separation, so that the separation effect of C6+ can be effectively improved;
finally, the separation of C4, C5-C6 and C6+ in the process by-products of propylene and ethylene preparation by catalytic cracking of olefin is realized through the separation device of the dehexanizer, the 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 or technical solutions in the prior art of the present invention, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained based on these drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a fine separation apparatus for an olefin catalytic cracking product in an embodiment.
Wherein, 1 is a depropanizer, 2 is a depropanizer, 3 is a feeding hole of the depropanizer, 4 is a reboiler, 5 is a reboiler returning hole, 6 is a flow valve, 7 is a reboiler removing hole, 8 is a depropanizer steam condensate tank, 9 is a depropanizer kettle liquid pump, 10 is a depropanizer kettle liquid cooler, 11 is a depropanizer kettle liquid after cooler, 12 is a product tank, 13 is a kettle discharging hole, 14 is a tower top gas phase outlet, 15 is a depropanizer condenser, 16 is a reflux tank of the depropanizer, 17 is an OCC device, 18 is a reflux pump, 19 is a pipeline I, 20 is a tower top reflux hole, 21 is a pipeline II, 22 is the debutanizer, 23 is a liquid level meter hole, 24 is a thermometer hole, and 25 is a safety valve at the tower top.
Detailed Description
In order to make those skilled in the art better understand the technical solution of the present invention, the technical solution in the embodiment of the present invention will be clearly and completely described below with reference to the drawings in the embodiment of the present invention, and it is obvious that the described embodiment is only a part of the embodiment of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In the description of the present invention, it is to 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 those shown in the drawings, and are used for descriptive purposes only to simplify the description of the present invention, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and therefore, are not to be construed as limiting the present invention.
As can be seen from the attached drawing, the separation method of the fine separation device for the 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 hole 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 tower inside the depropanizer 2 is 0.3MPaG, the separation of gas phase and liquid phase is realized, the gas phase kettle material is mainly C4-C6, and the liquid phase kettle material is C6 +; wherein, the reboiler 4 is of a vertical thermal siphon type, the heat source adopts 1.0MPaG low-pressure steam, the dehexanizer is provided with a reboiler return port 5 and a reboiler removal port 7, the heat exchange between the liquid in the dehexanizer and the steam is realized to realize the heating function of the reboiler, and the reboiler 4 is communicated with a dehexanizer steam condensate tank 8;
(2) discharging the liquid phase kettle material in the step (1) from a tower kettle discharge hole 13, boosting the pressure to 0.79MPaG by a dehexanizer kettle liquid pump 9, sequentially performing two-stage cooling by a dehexanizer kettle liquid cooler 10 and a dehexanizer kettle liquid aftercooler 11, cooling to 40 ℃, and conveying to a C6+ product tank 12; the flow rate of the discharge port 13 of the tower kettle and the liquid level of the dehexanizer tower kettle are controlled by a flow valve positioned at the discharge port 13 of the tower kettle;
(3) after the gas phase kettle materials (C4-C6) in the step (1) are discharged from a gas phase outlet 14 at the top of the tower, the gas phase kettle materials are firstly cooled by circulating cooling water through a dehexanizer condenser 15, the condensation temperature is 52.3 ℃, and then the gas phase kettle materials enter a dehexanizer reflux tank 16 for gas-liquid separation, the gas phase materials (mostly C4-C6 mono-olefins) are discharged from a gas phase outlet of the dehexanizer reflux tank 16 and enter the upstream of an OCC device 17 as reaction raw materials, the gas phase outlet is provided with a flow valve 6, and the liquid phase materials are discharged from a liquid phase outlet and enter a reflux pump 18;
(4) and (3) raising the pressure to 0.64MpaG by a reflux pump 18, pumping one part of the liquid-phase material in the step (3) to a reflux port 20 at the top of the tower through a pipeline I19 and entering a dehexanizer 2 for reflux recirculation, pumping the other part of the liquid-phase material to a debutanizer 22 through a pipeline II 21 as a feed material for C4 separation, and controlling the flow rate of the pipeline II 21 and the liquid level in a reflux tank 16 of the dehexanizer through a flow valve 6 positioned in the pipeline II 21.
In addition, the dehexanizer is also provided with a liquid level meter port 23, a thermometer port 24 and a tower top safety valve 25.
According to the fine separation device for the olefin catalytic cracking product, the separation of C4, C5-C6 and C6+ of OCC technical byproducts is realized through the separation method, the fine separation of C6+ is further realized, 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.
Although the present invention has been described in detail by referring to the drawings in connection with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and scope of the present invention, and these modifications or substitutions are within the scope of the present invention/any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.
Claims (9)
1. The fine separation device for the catalytic cracking products of the olefins comprises a separation system and is characterized in that: a hexane removal device is additionally arranged between a depropanizer and a debutanizer in a separation system, the hexane removal device comprises a dehexanizer, and the dehexanizer comprises a feed inlet, a tower top gas phase outlet, a tower bottom discharge port, a tower top reflux port, a reboiler outlet, a liquid level meter port, a thermometer port and a tower top safety valve; the bottom of the dehexanizer is connected with a reboiler; the discharge end of the depropanizing tower is communicated with the feed inlet of the depropanizing tower, the discharge port of the tower kettle is sequentially communicated with a depropanizing tower kettle liquid pump and a depropanizing tower kettle liquid cooling device through a pipeline, and the discharge end of the depropanizing tower kettle liquid cooling device is communicated with a product tank; the top of the tower gas phase export UNICOM has the dehexane tower condenser, and the discharge end UNICOM of dehexane tower condenser has the dehexane tower reflux tank, the dehexane tower reflux tank is equipped with gas phase export and liquid phase export, gas phase export and OCC device upstream UNICOM, and the liquid phase export UNICOM has the backwash pump, and the discharge end of backwash pump is equipped with pipeline I and pipeline II, pipeline II and the feed end UNICOM of debutanizer, pipeline I and top of the tower backward flow mouth UNICOM.
2. The apparatus for finely separating an olefin catalytic cracking product as claimed in claim 1, wherein: and a tower kettle discharge port of the dehexanizer and a pipeline II are provided with flow valves.
3. The apparatus for finely separating an olefin catalytic cracking product as claimed in claim 1, wherein: the reboiler is vertical thermosyphon reboiler, the reboiler is equipped with low pressure steam inlet and steam outlet, and steam outlet UNICOM has the dehexanizer steam condensate jar, and the dehexanizer steam condensate jar is equipped with the steam condensate export.
4. The apparatus for finely separating an olefin catalytic cracking product as claimed in claim 1, wherein: the de-hexane tower bottom liquid cooling device comprises a de-hexane tower bottom liquid cooler and a de-hexane tower bottom liquid aftercooler which are sequentially communicated through pipelines.
5. The apparatus for finely separating an olefin catalytic cracking product as claimed in claim 1, wherein: the condenser of the dehexanizer is provided with a circulating water cooling device.
6. A separation method suitable for the apparatus for finely separating an olefin catalytic cracking product according to 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 depropanizing tower enters the depropanizing tower from a feed inlet of the depropanizing tower, the temperature in the depropanizing tower is gradually increased under the action of a reboiler to realize the separation of gas phase and liquid phase, C4-C6 is changed into gas phase kettle material, and C6+ is changed into liquid phase kettle material;
(2) discharging the liquid phase kettle material in the step (1) from a discharge hole of the tower kettle, boosting the pressure by a liquid pump of the tower kettle, pumping the liquid phase kettle material to a de-hexane tower kettle liquid cooling device for cooling, and then conveying the liquid phase kettle material to a product tank of C6 +;
(3) after being discharged from a gas phase outlet at the top of the tower, the gas phase kettle material in the step (1) is firstly cooled by a dehexanizer condenser, and then enters a reflux tank of the dehexanizer for gas-liquid separation, the gas phase material is discharged from a gas phase outlet of the reflux tank of the dehexanizer and enters the upper stream of an OCC device as a reaction raw material, and the liquid phase material is discharged from 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 reflux port at the top of the tower through a pipeline I by the aid of a reflux pump for reflux recirculation, and pumping the other part of the liquid-phase material to a debutanizer through a pipeline II for feeding.
7. The method for separating an olefin catalytic cracking product fine separation device according to claim 6, wherein: the pressure at the top of the internal tower of the dehexanizer is 0.3 MPaG; a condenser of the dehexanizer is cooled by circulating water, and the condensation temperature is 52.3 ℃; the pumping pressure of the reflux pump is 0.64 MpaG; the pumping pressure of the dehexanizer bottoms pump is 0.79 MPaG; the product temperature of C6+ is cooled by the dehexanizer kettle liquid cooling equipment to be 40 ℃.
8. The method for separating an olefin catalytic cracking product fine separation device according to claim 6, wherein: the flow rate of the discharge hole of the tower kettle and the liquid level of the dehexanizer tower kettle are controlled by a flow valve positioned at the discharge hole of the tower kettle; and the flow of the pipeline II and the liquid level in the reflux tank of the dehexanizer are controlled by a flow valve positioned on the pipeline II.
9. The method for separating an olefin catalytic cracking product fine separation device according to claim 6, wherein: and (3) the liquid-phase kettle material discharged by the tower kettle liquid pump in the step (2) is sequentially subjected to two-stage cooling by a dehexanizer kettle liquid cooler and a dehexanizer kettle liquid aftercooler, and then is conveyed to a product tank of C6 +.
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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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Patent 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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