CN219149706U - Device for recovering effective components in olefin copolymer exhaust gas - Google Patents
Device for recovering effective components in olefin copolymer exhaust gas Download PDFInfo
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Abstract
An apparatus for recovering an effective component in an olefin copolymer exhaust gas, comprising a light component separation column; a heavy component separation column; the first inlet end of the exhaust gas absorption unit is communicated with the outlet end of the light component separation tower, and the second inlet end of the exhaust gas absorption unit is communicated with the outlet end of the heavy component separation tower; the at least two stages of flash tanks are a first stage flash tank and a second stage flash tank respectively, the inlet end of the first stage flash tank is communicated with the outlet end of the exhaust gas absorption unit, the outlet end of the bottom of the first stage flash tank is communicated with the inlet end of the second stage flash tank, and the outlet end of the bottom of the second stage flash tank is communicated with the light component separation tower; and the inlet end of the separator is communicated with the outlet end of the top of the second-stage flash tank. Compared with the prior art, the utility model can improve the recovery efficiency of the effective components and simultaneously can directly participate in the cyclic reaction of the copolymer.
Description
Technical Field
The utility model belongs to the technical field of polymer preparation, and particularly relates to a device for recycling effective components in olefin copolymer exhaust gas.
Background
The olefin copolymer is a high molecular compound formed by the polyaddition of various polymerization monomers (such as ethylene, propylene, 1-butene, 1-pentene, 1-octene, and the like), and is generally obtained by the polyaddition of two or more olefin monomers, and there are usually ethylene and 1-butene copolymer, ethylene and 1-octene copolymer, propylene and 1-octene copolymer, and the like. The polymerization process of olefin copolymers has been mature over long periods of time, and common polymerization processes include gas phase polymerization, slurry polymerization, solution polymerization, bulk polymerization, and the like. In the case of olefin copolymer elastomers, the light component monomer (light component monomer means olefin having 4 or less carbon atoms) used is ethylene or propylene, and the heavy component comonomer (heavy component comonomer means alpha olefin having 8 or more carbon atoms) is 1-octene, 1-decene, or the like.
Regardless of the above polymerization process, the olefin copolymer production process is required to solve the common problem of effluent gas treatment. When the olefin copolymer reaction catalyst system is mature, the single pass conversion rate in the polymerization process is still limited, and after the olefin monomer which does not participate in the reaction leaves the reaction kettle, the olefin monomer needs to be pressurized as recycle gas and then returns to the reaction kettle for continuous reaction, so that the high monomer conversion rate of the final polyaddition reaction is ensured. The polyaddition of polymers is a complex process, and during the circulation of recycle gas, the enrichment phenomenon of inert gases (such as reaction byproducts, small molecular alkanes of 1-6 carbon atoms such as ethane, propane, and the like, nitrogen, and the like) can occur. The enrichment of inert gas in the reaction kettle has a remarkable influence on the partial pressure control of the hydrogen in the reaction kettle, and the partial pressure control of the hydrogen in the reaction kettle is a main means for regulating and controlling the molecular weight of the olefin copolymer. In order to avoid enrichment of inert gases, it is often necessary to treat a portion of the recycle gas as vent gas in the polymerization process of olefin copolymers. The concentration of the hydrocarbon component is usually 5-40% of the total amount of the discharged gas, and the amount of ethylene and propylene contained in the discharged gas is about 0.4-1% of the yield of the olefin copolymer. In the early olefin copolymer device, the exhaust gas is generally introduced into a torch system for burning, so that a great amount of olefin monomers are wasted, and the problems of environmental pollution and the like are also caused in the torch burning process. Therefore, the recovery of the effective components (monomers such as ethylene, propylene and the like and solvents such as hexane and the like) in the exhaust gas can obviously reduce the unit consumption of the device, improve the economic benefit and reduce the pollution problem to the environment.
At present, the treatment means of the discharged gas of the olefin copolymer is greatly developed, and the olefin copolymer device usually adopts pressure swing adsorption (PSA for short), membrane separation, compression condensation, cryogenic method and other means to treat the discharged gas, but the methods have large recovery rate of effective components, energy consumption and investment difference, and various problems exist in practical use.
The Chinese patent No. ZL201110225097.2 (issued to No. CN 102389682B) discloses a method for treating high-pressure and low-pressure olefin copolymer exhaust gas generated in the production process of polyethylene and polypropylene, which adopts a pressure swing adsorption process flow, uses at least 4 refining beds filled with adsorbents, and sequentially subjects each refining bed to the steps of low-pressure adsorption, high-pressure adsorption, sequential release 1, concentration, vacuumizing, vacuum cleaning and pressurizing. The method can realize the separation of hydrocarbon, nitrogen and hydrogen through pressure swing adsorption, but the method can not realize the separation of olefin and alkane, and the recovered hydrocarbon-rich gas can only be sent to a cracking plant for recovery treatment or condensation recovery, and can not participate in the cyclic reaction.
Another example is chinese patent No. ZL200910038599.7, which discloses a method for completely recycling tail gas of a polyethylene device (grant publication No. CN 101530711B), and the method adopts a combination of membrane separation technology and pressure swing adsorption technology. The process comprises the steps of sending the exhaust gas from a high-pressure condensate tank of a polyethylene device into a membrane separation recovery system, recovering a certain amount of ethylene, comonomer (butene, hexene and octene) and induced condensing agent (isopentane and hexane) to return to an inlet of a circulating compressor, introducing the exhaust gas subjected to membrane separation into a pressure swing adsorption system to adsorb hydrocarbon components, obtaining hydrogen and nitrogen, using the hydrogen and nitrogen as device purge gas, and desorbing the hydrogen and nitrogen by the pressure swing adsorption system under a vacuum condition to obtain hydrocarbon-rich gas as fuel gas for combustion. The method can realize hydrocarbon recovery, but has limited hydrocarbon recovery ratio for participating in cyclic reaction, and a large amount of hydrocarbon is still consumed as fuel.
Disclosure of Invention
The utility model aims to solve the technical problem of providing a device for recycling the effective components in the discharged gas of the olefin copolymer, so as to improve the recycling efficiency of the effective components and simultaneously enable the effective components to directly participate in the cyclic reaction of the copolymer.
The technical scheme adopted for solving the technical problems is as follows: an apparatus for recovering an effective component of an olefin copolymer effluent gas comprising:
the top of the light component separation tower is provided with an outlet end for outputting tail gas with light component monomers;
the top of the heavy component separation tower is provided with an outlet end for outputting a medium with heavy component comonomer;
it is characterized in that the method also comprises the following steps:
an exhaust gas absorption unit, a first inlet end of which is communicated with an outlet end of the light component separation tower, and a second inlet end of which is communicated with an outlet end of the heavy component separation tower;
the at least two stages of flash tanks are a first stage flash tank and a second stage flash tank respectively, wherein the inlet end of the first stage flash tank is communicated with the outlet end of the exhaust gas absorption unit, the outlet end of the bottom of the first stage flash tank is communicated with the inlet end of the second stage flash tank, and the outlet end of the bottom of the second stage flash tank is communicated with the light component separation tower;
and the separator is used for separating light component monomers in the gas phase component, the inlet end of the separator is communicated with the outlet end of the top of the second-stage flash tank, and the outlet end of the separator is connected to an outlet pipeline of the copolymer reaction unit or the light component separation tower.
Therefore, the heavy component comonomer can be used as an absorbent to effectively absorb the light component monomer discharged by the light component separation tower in the exhaust gas absorption unit, noncondensable gas (such as nitrogen and hydrogen) generated in the polymerization process is removed after primary flash evaporation, alkane can be efficiently removed after secondary flash evaporation and separation by the separator, and the effective light component monomer is obtained, so that the raw material unit consumption of the olefin copolymer device is reduced, and the economic benefit is improved. And the components output from the separator can directly participate in the cyclic reaction of the copolymer.
Preferably, the exhaust gas absorption unit is a high pressure mixer or a gas phase absorption column or a combination of both. The high-pressure mixer and the gas phase absorption tower are all in the prior art.
Preferably, a gas compressor and a first heater are sequentially arranged on a connecting pipeline between the outlet end of the light component separation tower and the first inlet end of the exhaust gas absorption unit, and the gas compressor is positioned at the upstream of the first heater;
and a pressurizing pump and a second heater are sequentially arranged on a connecting pipe between the outlet end of the heavy component separation tower and the second inlet end of the exhaust gas absorption unit, and the pressurizing pump is positioned at the upstream of the second heater.
The outlet pressure of the gas compressor is 2.7-3.1 MPa (A).
Preferably, a reflux tank is further arranged on a connecting pipeline between the outlet end of the light component separation tower and the first inlet end of the exhaust gas absorption unit, the reflux tank is positioned at the upstream of the gas compressor, the outlet end at the top of the reflux tank is communicated with the inlet end of the gas compressor, the first inlet end at the middle part of the reflux tank is communicated with the outlet end at the top of the light component separation tower, the second inlet end at the middle part of the reflux tank is communicated with the outlet end of the separator, and the outlet end at the bottom of the reflux tank is communicated with the inlet end at the upper part of the light component separation tower;
meanwhile, the outlet end of the gas compressor is connected with a circulating pipeline which is connected to the copolymer reaction unit.
In each of the above aspects, preferably, the separator is a membrane separator having a separation membrane, and the separation membrane is arranged to pass only the light component monomer.
Preferably, a first pressure reducing valve is arranged on a connecting pipe line between the inlet end of the separator and the outlet end of the top of the second-stage flash tank; and a second pressure reducing valve is arranged on a pipeline connected with the outlet end of the top of the first-stage flash tank.
The method for recycling the effective components in the olefin copolymer exhaust gas by adopting the device comprises the following steps:
1. mixing the tail gas with the light component monomer output by the outlet end of the light component separation tower and the medium with the heavy component comonomer output by the outlet end of the heavy component separation tower in the exhaust gas absorption unit, so that the heavy component comonomer in the medium is used as an absorbent to absorb the light component monomer in the tail gas, wherein the tail gas entering the exhaust gas absorption unit is a first material flow, the medium entering the exhaust gas absorption unit is a second material flow, the mass flow ratio of the first material flow to the second material flow is 1:2.1-1:3.3, the operating pressure of the exhaust gas absorption unit is 2.7-3.0 MPa (A), and the operating temperature is 240-270 ℃;
2. the fluid output from the outlet end of the exhaust gas absorption unit enters a first-stage flash tank to carry out first-stage flash evaporation, the gas phase component after the first-stage flash evaporation is used as exhaust gas to be emptied, the liquid phase component after the first-stage flash evaporation enters a second-stage flash tank to carry out second-stage flash evaporation, the gas phase component after the second-stage flash evaporation enters a separator, the required effective component is output from the outlet end of the separator, the liquid phase component after the second-stage flash evaporation is conveyed to the light component separation tower, wherein the pressure of the first-stage flash evaporation is 0.4-0.6 MPa (A), and the pressure of the second-stage flash evaporation is 0.15-0.25 MPa (A).
"A" in MPa (A) in the above pressure unit means absolute pressure.
Preferably, the light component monomer is olefin with 2-4 carbon atoms; the heavy component comonomer is olefin with the carbon number of more than or equal to 8.
Preferably, the light component monomer is ethylene; the heavy component comonomer is 1-octene.
Compared with the prior art, the utility model has the advantages that: by additionally arranging the exhaust gas absorption unit, the at least two-stage flash tank and the separator on the basis of the existing light component separation tower and heavy component separation tower, the heavy component comonomer can be used as an absorbent to effectively absorb the light component monomer discharged by the light component separation tower in the exhaust gas absorption unit, noncondensable gas (such as nitrogen and hydrogen) generated in the polymerization process is removed after primary flash evaporation, alkane can be efficiently removed after secondary flash evaporation and separation by the separator, and the effective light component monomer is obtained, so that the raw material unit consumption of the olefin copolymer device is reduced, and the economic benefit is improved. And the components output from the separator can directly participate in the cyclic reaction of the copolymer.
Drawings
FIG. 1 is a schematic structural diagram of embodiment 1 of the present utility model;
fig. 2 is a schematic structural diagram of embodiment 4 of the present utility model.
Detailed Description
The utility model is described in further detail below with reference to the embodiments of the drawings.
Example 1:
as shown in FIG. 1, there is shown a preferred embodiment 1 of the apparatus for recovering an effective component in an olefin copolymer exhaust gas of the present utility model, which comprises a light component separation column 1, a heavy component separation column 2, an exhaust gas absorption unit 3, a flash tank and a separator 6.
Wherein the top of the light component separation tower 1 is provided with an outlet end for outputting tail gas with light component monomers.
The top of the heavy component separation column 2 has an outlet end for the medium output with heavy component comonomer.
In this embodiment, as in the prior art, the bottom of the light component separation column 1 is connected to the heavy component separation column 2 after passing through the primary separation system 7 and the solvent separation system 8 in this order.
The exhaust gas absorption unit 3 is a high-pressure mixer, a first inlet end of which is communicated with the outlet end of the light component separation tower 1, and a second inlet end of which is communicated with the outlet end of the heavy component separation tower 2. Wherein, be equipped with reflux drum 13, gas compressor 11 and first heater 12 in proper order on the connecting line between the exit end of light component knockout drum 1 and the first entry end of exhaust gas absorption unit 3, gas compressor 11 is located the upper reaches of first heater 12 to be located the low reaches of reflux drum 13, the exit end at reflux drum 13 top is linked together with the entry end of gas compressor 11, the entry end in the middle part of reflux drum 13 is linked together with the exit end at light component knockout drum 1 top, the exit end at reflux drum 13 bottom is linked together with the entry end at light component knockout drum 1 upper portion. Meanwhile, the outlet end of the gas compressor 11 is connected with a circulation line 111, and the circulation line 111 is connected to the copolymer reaction unit. A pressurizing pump 21 and a second heater 22 are sequentially provided on a connection line between the outlet end of the heavy component separation column 2 and the second inlet end of the exhaust gas absorption unit 3, and the pressurizing pump 21 is located upstream of the second heater 22.
The flash tank is provided with two stages, namely a first-stage flash tank 4 and a second-stage flash tank 5, wherein the inlet end of the first-stage flash tank 4 is communicated with the outlet end of the exhaust gas absorption unit 3, a second pressure reducing valve 41 is arranged on a pipeline connected with the outlet end at the top of the first-stage flash tank 4, the outlet end at the bottom of the first-stage flash tank 4 is communicated with the inlet end of the second-stage flash tank 5, and the outlet end at the bottom of the second-stage flash tank 5 is communicated with the light component separation tower 1.
The separator 6 described above is a membrane separator having a separation membrane, and the separation membrane is arranged to pass only the light component monomer. The inlet end of the separator 6 is communicated with the outlet end at the top of the second-stage flash tank 5, and a first pressure reducing valve 51 is arranged on the communicating pipe; the outlet end of the separator 6 is connected to the inlet end of the middle part of the reflux drum 13.
The second pressure reducing valve 41 is depressurized to 0.5MPa (A), and the exhaust gas discharged from the outlet end of the top of the first-stage flash tank can enter a flare system for combustion treatment.
The first pressure reducing valve 51 reduces the pressure to 0.23MPa (A).
The method for recovering the effective components in the olefin copolymer exhaust gas by using the apparatus of this example comprises the following steps:
1. the tail gas (the temperature is 30 ℃ and the pressure is 0.2MPa (A)) with the light component monomer (ethylene) output from the outlet end of the light component separation tower 1 and the medium (the pressure is 1-octene) with the heavy component comonomer (1-octene) output from the outlet end of the heavy component separation tower 2 are respectively boosted and heated and then mixed in the exhaust gas absorption unit 3, so that the heavy component comonomer in the medium is used as an absorbent to absorb the light component monomer in the tail gas, wherein the tail gas entering the exhaust gas absorption unit 3 is a first stream, the medium entering the exhaust gas absorption unit 3 is a second stream, the flow of the first stream is 1873kg/h, the flow of the second stream is 3933.3kg/h, the operating pressure of the exhaust gas absorption unit 3 is 2.7MPa (A), and the operating temperature is 244 ℃;
2. the fluid output from the outlet end of the exhaust gas absorption unit 3 enters a first-stage flash tank 4 for primary flash evaporation, the gas phase component after primary flash evaporation is used as exhaust gas for emptying, the liquid phase component after primary flash evaporation enters a second-stage flash tank 5 for secondary flash evaporation, the gas phase component after secondary flash evaporation enters a separator 6, the required effective component is output from the outlet end of the separator 6, the liquid phase component after secondary flash evaporation is conveyed to the light component separation tower 1, wherein the pressure of the primary flash evaporation is 0.5MPa (A), and the pressure of the secondary flash evaporation is 0.23MPa (A).
The results of this example are shown in table 1 below, wherein "inlet tail gas" in the table refers to the first stream; "recovered light hydrocarbon gas" refers to the stream output from the outlet end of separator 6; "vent gas" refers to the stream exiting the outlet end at the top of the first stage flash tank 4; "recovery liquid" refers to the stream that is output from the outlet end of the bottom of the second stage flash tank 5.
TABLE 1
The present utility model introduces an effluent gas absorbing unit 3 and a flash separation unit (as defined by the dashed box in fig. 1) on the original olefin copolymer plant. Based on the principle of similar miscibility, the heavy component comonomer 1-octene is selected as an absorbent to effectively absorb and discharge the monomer ethylene in the tail gas (namely the first stream). The liquid phase absorption of ethylene essentially belongs to the physical absorption process, the gas phase partial pressure of ethylene is increased, namely the mass transfer driving force is increased, the low temperature is favorable for improving the solubility of ethylene, and the operation conditions of low temperature and high pressure are selected, so that the effective components of the tail gas are favorably absorbed.
The critical pressure, critical temperature, boiling point data for several components of the present utility model are shown in table 2 below:
TABLE 2
In the utility model, the operation temperature of the exhaust gas absorption unit 3 is higher than the critical temperature of ethylene, propylene and normal hexane, lower than the critical temperature of 1-octene, and the operation pressure is higher than the critical pressure of 1-octene and lower than the critical pressure of ethylene, propylene and normal hexane. The effective components and the absorbent in the tail gas are in subcritical state, the effective components cannot be liquefied, and the absorbent cannot be gasified. In subcritical state, molecular diffusion performance of ethylene, propylene and the like is obviously enhanced, mass transfer speed is accelerated, and compared with other conventional absorption unit operation, good absorption effect can be expected.
The utility model preferably uses 1-octene as absorbent, besides good solubility to ethylene, also has the advantages of high boiling point (122-123 ℃) and gasification, if the absorbent (such as hexane) with lower boiling point is used, a large amount of absorbent is gasified by flash separation, the separation effect is seriously reduced, and thus the economy of separation operation is reduced.
The utility model adopts two-stage flash evaporation, and aims to recover the effective components (ethylene and hexane) in the exhaust gas to the greatest extent, noncondensable gas (nitrogen and hydrogen) accumulated in the production process of the primary flash evaporation removing device is removed, and the secondary flash evaporation is used for efficiently removing alkane by the separator 6, so that the raw material unit consumption of the olefin copolymer device is reduced, and the economic benefit is improved.
Example 2:
this example is substantially the same as example 1, except that the process parameters are different, in this example, the flow rate of the second stream in the first step is 5244.4kg/h, and the results of this example are shown in the following table 3:
TABLE 3 Table 3
Example 3:
this example is substantially the same as example 1 except that the process parameters are different, in this example, the operating pressure of the exhaust gas absorption unit 3 in step one is 2.9MPa (a) and the operating temperature is 248 ℃; the second stream was 5244.4kg/h and the results of this example are shown in Table 4 below:
TABLE 4 Table 4
The analysis of examples 1 to 3 above was performed as follows:
| hydrocarbon recovery% | Exhaust gas flow rate kg/h | |
| Example 1 | 78.07 | 1341.9 |
| Example 2 | 84.13 | 1305.76 |
| Example 3 | 89.25 | 1285.53 |
According to the three embodiments, the method for recycling the effective components of the exhaust gas by using the heavy component comonomer can realize the efficient recycling of the effective components of the exhaust gas, meanwhile, a medium of a non-reaction system is not required to be introduced, the recycling amount of hydrocarbons is high, the energy consumption investment is saved, and the unit consumption of the reaction is reduced.
Example 4:
as shown in fig. 2, which is a preferred embodiment 4 of the apparatus for recovering an effective component in an olefin copolymer exhaust gas of the present utility model, this embodiment is substantially the same as embodiment 1 except that the exhaust gas absorbing unit 3 is a gas phase absorbing tower in this embodiment. The results of this example are shown in table 5 below:
TABLE 5
Example 5:
the difference between this embodiment and embodiment 1 is that in this embodiment, the exhaust gas absorption unit 3 is a combination of a high-pressure mixer and a gas phase absorption tower, the two are connected in series, the first stream and the second stream enter the high-pressure mixer to be absorbed once, then enter the gas phase absorption tower to be absorbed twice, the stream after the absorption twice is subjected to subsequent flash evaporation treatment, and the pressure in the high-pressure mixer is 3.1MPa (a), and the operation temperature is 263 ℃; the pressure in the gas phase absorption tower was 3.0MPa (A), slightly lower than the pressure in the high pressure mixer, and the operating temperature in the gas phase absorption tower was 262 ℃. The results of this example are shown in table 6 below:
TABLE 6
Example 6:
this example is substantially the same as example 1 except that the process parameters are different, in this example, the operating pressure of the exhaust gas absorption unit 3 in step one is 3.0MPa (a) and the operating temperature is 270 ℃; the pressure of the primary flash evaporation in the second step is 0.4MPa (A), and the pressure of the secondary flash evaporation is 0.15MPa (A). The results of this example are shown in table 7 below:
TABLE 7
Example 7:
this example is substantially the same as example 1 except that the process parameters are different, in this example, the operating pressure of the exhaust gas absorption unit 3 in step one is 2.8MPa (a) and the operating temperature is 240 ℃; the pressure of the primary flash evaporation in the second step is 0.6MPa (A), and the pressure of the secondary flash evaporation is 0.25MPa (A). The results of this example are shown in table 8 below:
TABLE 8
The above examples 3 to 7 were analyzed and the results were as follows:
| hydrocarbon recovery% | Exhaust gas flow rate kg/h | |
| Example 3 | 89.25 | 1285.53 |
| Example 4 | 73.52 | 1356.2 |
| Example 5 | 86.67 | 1306.7 |
| Example 6 | 74.27 | 1360.8 |
| Example 7 | 79.18 | 1328.2 |
As can be seen from the above examples 3 to 7, the method for recovering the effective components of the exhaust gas by using the heavy component comonomer can realize the efficient recovery of the effective components of the exhaust gas, meanwhile, a medium which is not a reaction system is not required to be introduced, the recovery amount of hydrocarbons is very high, the energy consumption investment is saved, and the unit consumption of the reaction is reduced. In particular, example 5 uses a combination of a vapor phase absorber and a high pressure mixer to achieve higher hydrocarbon recovery with less heavy component absorption monomer than in example 3.
Claims (6)
1. An apparatus for recovering an effective component of an olefin copolymer effluent gas comprising:
a light component separation tower (1), the top of which is provided with an outlet end for outputting tail gas with light component monomers;
a heavy component separation column (2) having an outlet end at the top for the medium output with heavy component comonomer;
it is characterized in that the method also comprises the following steps:
the first inlet end of the exhaust gas absorption unit (3) is communicated with the outlet end of the light component separation tower (1), and the second inlet end of the exhaust gas absorption unit is communicated with the outlet end of the heavy component separation tower (2);
the system comprises at least two stages of flash tanks, namely a first stage flash tank (4) and a second stage flash tank (5), wherein the inlet end of the first stage flash tank (4) is communicated with the outlet end of the exhaust gas absorption unit (3), the outlet end of the bottom of the first stage flash tank (4) is communicated with the inlet end of the second stage flash tank (5), and the outlet end of the bottom of the second stage flash tank (5) is communicated with the light component separation tower (1);
and the separator (6) is used for separating light component monomers in the gas phase component, the inlet end of the separator is communicated with the outlet end at the top of the second-stage flash tank (5), and the outlet end of the separator is connected to an outlet pipeline of the copolymer reaction unit or the light component separation tower (1).
2. The apparatus according to claim 1, wherein: the exhaust gas absorption unit (3) is a high-pressure mixer or a gas phase absorption tower or a combination of the two.
3. The apparatus according to claim 1, wherein: a gas compressor (11) and a first heater (12) are sequentially arranged on a connecting pipeline between the outlet end of the light component separation tower (1) and the first inlet end of the exhaust gas absorption unit (3), and the gas compressor (11) is positioned at the upstream of the first heater (12);
a pressurizing pump (21) and a second heater (22) are sequentially arranged on a connecting pipeline between the outlet end of the heavy component separation tower (2) and the second inlet end of the exhaust gas absorption unit (3), and the pressurizing pump (21) is positioned at the upstream of the second heater (22).
4. A device according to claim 3, characterized in that: a reflux tank (13) is further arranged on a connecting pipeline between the outlet end of the light component separation tower (1) and the first inlet end of the exhaust gas absorption unit (3), the reflux tank (13) is positioned at the upstream of the gas compressor (11), the outlet end at the top of the reflux tank (13) is communicated with the inlet end of the gas compressor (11), the first inlet end at the middle part of the reflux tank (13) is communicated with the outlet end at the top of the light component separation tower (1), the second inlet end at the middle part of the reflux tank (13) is communicated with the outlet end of the separator (6), and the outlet end at the bottom of the reflux tank (13) is communicated with the inlet end at the upper part of the light component separation tower (1);
meanwhile, a circulation line (111) is connected to the outlet end of the gas compressor (11), and the circulation line (111) is connected to the copolymer reaction unit.
5. The apparatus according to any one of claims 1 to 4, wherein: the separator (6) is a membrane separator having a separation membrane and the separation membrane is arranged to pass only light fraction monomers.
6. The apparatus according to claim 5, wherein: a first pressure reducing valve (51) is arranged on a connecting pipe line between the inlet end of the separator (6) and the outlet end of the top of the second-stage flash tank (5); and a second pressure reducing valve (41) is arranged on a pipeline connected with the outlet end at the top of the first-stage flash tank (4).
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