CN215162247U - Propylene recovery device of epoxypropane styrene coproduction system - Google Patents
Propylene recovery device of epoxypropane styrene coproduction system Download PDFInfo
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- CN215162247U CN215162247U CN202120673135.XU CN202120673135U CN215162247U CN 215162247 U CN215162247 U CN 215162247U CN 202120673135 U CN202120673135 U CN 202120673135U CN 215162247 U CN215162247 U CN 215162247U
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Abstract
The utility model provides a propylene recovery unit of epoxypropane styrene coproduction system mainly comprises high-pressure propylene recovery tower, noncondensable gas desorption tower, depropanization tower, flash distillation washing jar, low pressure propylene recovery tower and propylene compressor. The utility model discloses can the efficient retrieve the back with excessive propylene in the propylene epoxidation result, return the reactor and continue to participate in the reaction, will not congeal gas discharge system simultaneously, not only reduced the reaction raw materials consumption, also alleviateed the flammable and explosive tail gas treatment load of device simultaneously to the effectual long-term operation of having avoided in the noncondensable gas accumulation in the system lead to operating pressure to rise, cause the problem that propylene gas discharge torch volume increases and system energy consumption increases.
Description
Technical Field
The utility model belongs to the technical field of chemical production, especially, relate to a propylene recovery unit of epoxypropane styrene coproduction system.
Background
Propylene oxide, also known as propylene oxide, methyl ethylene oxide, is a very important organic compound starting material, second only to polypropylene and acrylonitrile, the third largest propylene derivative. The propylene oxide is mainly used for producing polyether polyol, propylene glycol, various nonionic surfactants and the like, wherein the polyether polyol is an important raw material for producing polyurethane foam, heat insulation materials, elastomers, adhesives, coatings and the like, and the various nonionic surfactants are widely applied to industries such as petroleum, chemical engineering, pesticides, textile, daily chemicals and the like. Meanwhile, propylene oxide is also an important basic chemical raw material.
Styrene is an organic compound formed by substituting one hydrogen atom of ethylene with benzene, and the electron of vinyl is conjugated with a benzene ring, and is one of aromatic hydrocarbons. The molecular formula is C8H8, and the structural formula is C6H5CH ═ CH 2. Is present in storax, a natural perfume. Colorless and oily liquid with special fragrance. Melting point-30.6 deg.C, boiling point 145.2 deg.C, relative density 0.9060 (20/4 deg.C), refractive index 1.5469chemical book, viscosity 0.762cPat68 deg.F. It is insoluble in water, soluble in alcohol and ether, and exposed to air to generate polymerization and oxidation gradually, and can be stored only by adding polymerization inhibitor (hydroquinone or tert-butyl catechol (0.0002% -0.002) as stabilizer to delay its polymerization). Industrially, they are important monomers for synthetic resins, ion exchange resins, synthetic rubbers and the like.
Under specific reaction temperature and pressure, ethylbenzene is oxidized by oxygen in a liquid phase reactor to generate ethylbenzene hydroperoxide (EBHP), the generated ethylbenzene hydroperoxide is concentrated to a certain concentration and then enters an epoxidation process, and under the specific reaction temperature and reaction pressure, the ethylbenzene hydroperoxide and propylene undergo epoxidation reaction to generate propylene oxide and phenethyl alcohol. And distilling the epoxidation reaction liquid to obtain propylene oxide, and dehydrating phenethyl alcohol to generate styrene. The PO/SM coproduction method is characterized in that high-temperature reaction is not needed, and two important organic chemical products of styrene and propylene oxide can be coproduced simultaneously. The two reactions of heat absorption of ethylbenzene dehydrogenation and heat release of propylene oxidation are combined, so that energy is saved, and the problem of three-waste treatment in the production of propylene oxide is solved. In addition, the investment cost of the co-production device is reduced by 25 percent compared with the single propylene oxide and styrene device, and the operation cost is reduced by more than 50 percent, so the method has more competitive advantage when being used for building large-scale production devices.
Propylene feeding of the propylene epoxidation reactor is excessive in propylene epoxidation reaction, the utility model provides a method for recovering excessive propylene in the propylene epoxidation reactor and simultaneously removing non-condensed steam and propane and hydrocarbon heavy components above in the propylene.
Disclosure of Invention
In view of this, the utility model aims at overcoming the defect that exists among the above-mentioned prior art, provide a propylene recovery unit of high-efficient epoxypropane styrene coproduction system, return the reactor after retrieving excessive propylene high purity in the propylene epoxidation result and continue to participate in the reaction to carry into the not condensed steam in propane and above hydrocarbon heavy ends and the ethane and the system in the effectual desorption propylene feeding simultaneously.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
a propylene recovery device of an epoxypropane styrene co-production system comprises a high-pressure propylene recovery tower, wherein the high-pressure propylene recovery tower is connected with an input pipeline of a propylene epoxidation reaction product;
the conveying medium in the input pipeline of the propylene epoxidation reaction product is propylene, propane and hydrocarbon heavy components above, ethylene and other non-condensed steam and propylene epoxidation reaction products.
The top of the high-pressure propylene recovery tower is connected with a condenser through a fourteen conveying pipe, the bottom of the condenser is connected with a reflux tank through a fifteen conveying pipe, a gas phase outlet of the reflux tank is connected with a non-condensable gas removing tower in series, the top of the non-condensable gas removing tower is connected with a thirteen conveying pipe, the bottom of the reflux tank is connected with an eleven conveying pipe and a twelve conveying pipe, and the eleven conveying pipe is connected with a depropanizer;
the main media conveyed by the thirteen conveying pipes are ethane and other non-condensed steam, and the main media conveyed by the twelve conveying pipes are propylene with the purity of more than 99 percent;
the tower top of the depropanizing tower is connected with a high-pressure propylene recovery tower through a tenth conveying pipe, and the bottom of a tower kettle of the depropanizing tower is connected with a ninth conveying pipe;
the purity of the conveying medium of the tenth conveying pipe is more than 99.9 percent, and the conveying medium of the ninth conveying pipe is propane and hydrocarbon heavy components above.
The high pressure propylene recovery tower's tower bottom links to each other through the third conveyer pipe with the flash water washing jar, the top and the low pressure propylene recovery tower of flash water washing jar pass through the fourth conveyer pipe and link to each other, and the bottom and the low pressure propylene recovery tower of flash water washing jar pass through the fifth conveyer pipe and link to each other, the top of the tower gas phase product of low pressure propylene recovery tower links to each other with the high-pressure depropanizer after the compression of propylene compressor. And the bottom of the tower kettle of the low-pressure propylene recovery tower is connected with an eighth conveying pipe.
The third conveying pipe is used for conveying a medium which is a propylene and propylene epoxidation reaction product, the fourth conveying pipe is used for conveying a medium which is a propylene and propylene epoxidation reaction product gas phase, the fifth conveying pipe is used for conveying a medium which is a propylene and propylene epoxidation reaction product liquid phase, and the eighth conveying pipe is used for conveying a medium which is a propylene epoxidation reaction product.
Further, the input pipeline of the propylene epoxidation reaction product comprises a first delivery pipe and a second delivery pipe, and the first delivery pipe and the second delivery pipe are respectively connected with different tray positions of the high-pressure propylene recovery tower.
The first conveying pipe conveying medium is a gas phase and contains propylene, propane and hydrocarbon heavy components above, ethylene and other non-condensed steam, and the second conveying pipe conveying medium is a liquid phase and contains propylene and propylene epoxidation reaction products.
Furthermore, a fourth conveying pipe is connected with the upper tower plate of the low-pressure propylene recovery tower, a fifth conveying pipe is connected with the top of the low-pressure propylene recovery tower, and a fifth conveying pipe conveying medium provides effective cold input for rectification separation for the low-pressure propylene recovery tower.
Furthermore, a connecting pipeline between the tower top of the low-pressure propylene recovery tower and the high-pressure propylene recovery tower is provided with a propylene compressor, and the propylene compressor is connected with the low-pressure propylene recovery tower through a sixth conveying pipe and is connected with the high-pressure propylene recovery tower through a seventh conveying pipe.
The sixth conveying pipeline conveying medium is low-pressure propylene gas, and the seventh conveying pipeline conveying medium is high-pressure propylene gas.
Further, the operating pressure of the high-pressure propylene recovery column is 1.6 to 2.2MPaG in gauge pressure, the operating pressure of the low-pressure propylene recovery column is 0.1 to 0.4MPaG in gauge pressure, and the operating pressure of the depropanizer is 1.5 to 2.1MPaG in gauge pressure.
Further, the outlet pressure of the propylene compressor is 1.7 to 2.3MPaG in gauge pressure.
Further, the operation temperature of the tower kettle of the high-pressure propylene recovery tower is 100-140 ℃, and the operation temperature of the tower top of the high-pressure propylene recovery tower is 30-50 ℃.
Further, the tower kettle operation temperature of the depropanizing tower is 50-60 ℃, and the tower top operation temperature of the depropanizing tower is 30-50 ℃.
Furthermore, in the propylene epoxidation reaction product, the content of propylene is 40-86 percent, the content of hydrocarbon heavy components is 4-8 percent, the content of non-condensable gas is 0.1-1.5 percent, and the content of other components is 4-56 percent in percentage by weight.
Compared with the prior art, the beneficial effects of the utility model are that:
(1) this propylene recovery unit of epoxypropane styrene coproduction system has adopted two tower processes of high pressure propylene recovery tower + low pressure propylene recovery tower, and the purity of retrieving the propylene product has been guaranteed to the high pressure propylene recovery tower, and propylene recovery rate in the propylene cyclization product has been guaranteed to the low pressure propylene recovery tower.
(2) This propylene recovery unit of epoxypropane styrene coproduction system, depropanizer set up to the gaseous discharge port that provides of propane that raw materials propylene brought the system into, effectually avoided long-term operation propane gas to accumulate in the system and lead to the problem that propylene epoxidation reaction conversion reduces and propylene recovery system energy consumption increases.
(3) This propylene recovery unit of epoxypropane styrene coproduction system, noncondensable gas desorption tower set up to the raw materials and brought into the noncondensable gas that light component and system produced and provide the discharge port, and the effectual noncondensable gas that has avoided long-term operation accumulates in the system and leads to operating pressure to rise, causes the problem that propylene gas discharge torch volume increases and system energy consumption increases.
(4) This propylene recovery unit of epoxypropane styrene coproduction system, propylene product are from the output of reflux drum bottom, have overcome the side draw flow loaded down with trivial details, the complicated drawback of control.
(5) This propylene recovery unit of epoxypropane styrene coproduction system, high-pressure propylene recovery tower reflux drum gas phase outlet has set up a little non-condensing desorption tower, has realized the separation of non-condensing and propylene to the loss of propylene has been avoided.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without undue limitation. In the drawings:
FIG. 1 is a flow chart of a propylene recovery device of an epoxypropane styrene co-production system.
Description of reference numerals:
t101-high pressure propylene recovery column; t102-low pressure propylene recovery column; t103-depropanizer; t104-noncondensable gas removing tower; x101-flash water washing tank; a C101-propane compressor; e101-a condenser; v101-reflux drum;
101-a first delivery pipe; 102-a second delivery pipe; 103-a third delivery pipe; 104-a fourth delivery pipe; 105-a fifth delivery duct; 106-sixth delivery pipe; 107-seventh delivery tube; 108-an eighth delivery duct; 109-a ninth delivery duct; 110-tenth delivery pipe; 111-eleven delivery pipes; 112-twelve delivery pipes; 113-thirteen delivery tubes; 114-fourteen delivery tubes; 115-fifteen ducts.
Detailed Description
It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The invention will be described in detail with reference to the following examples with reference to the accompanying drawings: as shown in fig. 1, the present embodiment provides a propylene recovery device of an epoxypropane and styrene co-production system, which includes a high-pressure propylene recovery tower T101, a low-pressure propylene recovery tower T102, a depropanizer T103, a non-condensable gas stripper T104, a flash water washing tank X101, a propylene compressor, a condenser E101, and a reflux tank V101;
specifically, a first delivery pipe 101 and a second delivery pipe 102 are connected to the high-pressure propylene recovery column T101, wherein the first delivery pipe 101 is connected to an upper tray of the high-pressure propylene recovery column T101 for delivering a propylene epoxidation gas-phase reaction product, the second delivery pipe 102 is connected to a lower tray of the high-pressure propylene recovery column T101 for delivering a propylene epoxidation liquid-phase reaction product, and the first delivery pipe 101 and the second delivery pipe 102 feed a propylene-containing raw material into the high-pressure propylene recovery column T101 from different positions for separation;
the operating pressure of the high-pressure propylene recovery tower T101 is 1.6-2.2 MPaG, the operating temperature of a tower kettle is 100-140 ℃, and the operating temperature of a tower top is 30-50 ℃. The product at the top of the high-pressure propylene recovery tower T101 is propylene, and the product at the bottom of the tower is an epoxidation reaction product containing a certain amount of propylene.
The top of a high-pressure propylene recovery tower T101 is connected with a condenser E101, the bottom of the condenser E101 is connected with a reflux tank V101, the gas-phase outlet of the reflux tank V101 is connected in series with a non-condensable gas removing tower T104, the top of the non-condensable gas removing tower T104 is connected with a thirteen conveying pipe 113 for conveying non-condensable gas, the bottom of the reflux tank V101 is connected with a middle tower plate of a depropanizer T103 through an eleven conveying pipe 111, and the eleven conveying pipe 111 is connected with a twelve conveying pipe 112;
the top of the depropanizer T103 is connected with the upper tray of the high-pressure propylene recovery tower T101 through a tenth delivery pipe 110, and the bottom of the tower kettle of the depropanizer T103 is connected with a ninth delivery pipe 109.
Because the propylene-containing raw material can carry trace light components, such as ethane, a small amount of non-condensable gas can be generated in the epoxidation reaction process, the system runs for a long time, and the pressure of the system is increased due to the accumulation of the non-condensable gas in the system, so that the system needs to be provided with a non-condensable gas discharge port. The utility model discloses gaseous phase export at reflux drum V101 has set up a miniature rectifying column as noncondensable gas desorption tower T104 for retrieve the propylene of smuggleing secretly in the noncondensable gas, retrieve propylene and return reflux drum V101, return high-pressure propylene recovery tower T101 through depropanization tower T103, or return propylene epoxidation reactor through twelve conveyer pipes 112, avoided the propylene loss, noncondensable gas then is discharged from the top of the tower of noncondensable gas desorption tower T104.
Because the raw material containing propylene contains a trace amount of propane, C4s and other hydrocarbon heavy components, the hydrocarbon heavy components can be accumulated in the system under long-term operation, so that the concentration of propylene is reduced, the conversion rate of propylene epoxidation reaction is influenced, and the energy consumption of a propylene recovery system is increased. In order to avoid the problem, the propylene product recovered from the top of the high-pressure propylene recovery tower T101 for removing the non-condensable gas is sent to a depropanizer T103 according to a certain proportion to remove hydrocarbon heavy components. The propylene product at the top of the depropanizing tower T103 returns to the high-pressure propylene recovery tower T101, the hydrocarbon heavy components are discharged from a system at the bottom of the depropanizing tower T103, the operating pressure of the depropanizing tower T103 is 1.5-2.1 MPaG, the operating temperature of the bottom of the depropanizing tower is 50-60 ℃, and the operating temperature at the top of the depropanizing tower is 30-50 ℃.
The bottom of the tower kettle of the high-pressure propylene recovery tower T101 is connected with the flash water washing tank X101 through a third conveying pipe 103 and is used for conveying byproducts of the high-pressure propylene recovery tower T101, the top of the flash water washing tank X101 is connected with the low-pressure propylene recovery tower T102 through a fourth conveying pipe 104 and is used for conveying flash vapor phase substances, and the bottom of the flash water washing tank X101 is connected with the top of a tower plate of the low-pressure propylene recovery tower T102 through a fifth conveying pipe 105 and is used for conveying liquid phase substances after flash water washing.
The top of the low-pressure propylene recovery tower T102 is connected with the upper tray of the high-pressure propylene recovery tower T101, the connecting pipeline of the low-pressure propylene recovery tower T102 and the high-pressure propylene recovery tower T101 is provided with a propylene compressor, the low-pressure propylene recovery tower T102 is connected with the propylene compressor through a sixth conveying pipe 106, the low-pressure propylene recovery tower T102 is used for conveying products at the top of the low-pressure propylene recovery tower T102, the propylene compressor is connected with the high-pressure propylene recovery tower T101 through a seventh conveying pipe 107, the low-pressure propylene recovery tower T102 is used for conveying boosted propylene gas, and the bottom of the tower kettle of the low-pressure propylene recovery tower T102 is connected with an eighth conveying pipe 108 and used for conveying epoxy reaction products.
In the using process, an epoxidation reaction product containing a certain amount of propylene is discharged from the tower bottom of the high-pressure propylene recovery tower T101 and enters a flash water washing tank X101, a flash vapor phase enters a low-pressure propylene recovery tower T102, and a liquid phase is washed by water and then enters the low-pressure propylene recovery tower T102 from different positions. The product at the top of the low-pressure propylene recovery tower T102 is recovered propylene gas, the product at the bottom of the tower is a propylene epoxidation reaction product for removing propylene, and the operating pressure of the low-pressure propylene recovery tower T102 is 0.1-0.4 MPaG.
Because the operation pressure of the low-pressure propylene recovery tower T102 is lower, the purity of the recovered propylene is not high enough, the propylene recovered from the tower top is pressurized by a propylene compressor C101 and then is sent to the high-pressure propylene recovery tower T101 as a feed, and the outlet pressure of the propylene compressor C101 is 1.7-2.3 MPaG.
The first embodiment is as follows:
take an example of a device designed on a scale of 10 ten thousand tons of propylene oxide to 22.5 ten thousand tons of styrene per year.
The gas-phase product and the liquid-phase product from the propylene epoxidation reaction respectively enter a high-pressure propylene recovery tower T101 from different positions, the operating pressure of the high-pressure propylene recovery tower T101 is 1.8MPaG, the tower bottom operating temperature is 130 ℃, and the tower top operating temperature is 46 ℃. The product at the top of the high-pressure propylene recovery tower T101 is recovered propylene, the recovered propylene is removed from non-condensed steam by a non-condensed steam removal tower T104, and then the propylene product with a certain proportion is removed from a depropanizer T103 by an eleven conveying pipe 111, and the recovered propylene returns to a propylene epoxidation reactor by a sixteen conveying pipe 116.
The propylene product at the top of the depropanizing tower T103 returns to the high-pressure propylene recovery tower T101 through a tenth conveying pipe 110, the hydrocarbon heavy component is discharged from the bottom of the depropanizing tower T103 through a ninth conveying pipe 109, the operating pressure of the depropanizing tower T103 is 1.75, the operating temperature of the bottom of the tower is 55 ℃, and the operating temperature at the top of the tower is 40 ℃.
The epoxidation reaction product containing a certain amount of propylene is discharged from the tower bottom of the high-pressure propylene recovery tower T101 and enters a flash water washing tank X101, a flash vapor phase enters a low-pressure propylene recovery tower T102, and a liquid phase is washed and also enters the low-pressure propylene recovery tower T102 from different positions. The product at the top of the low-pressure propylene recovery tower T102 is recovered propylene gas, the product at the bottom of the tower is a propylene epoxidation reaction product for removing propylene, and the operating pressure of the low-pressure propylene recovery tower is 0.25 MPaG. The product at the top of the low-pressure propylene recovery tower T102 is pressurized by a propylene compressor C101 and then is sent to the high-pressure propylene recovery tower T101 as a feed, and the outlet pressure of the propylene compressor C101 is 1.9 MPaG.
The composition parameters of the various streams are detailed in the following table:
| |
101 | 102 | 112 | 113 | 108 | 109 |
| Flow (kg/h) | 53210 | 204963 | 128771 | 250 | 129001 | 150 |
| Propylene (wt%) | 86％ | 40.5％ | 99.93％ | 30％ | 0％ | 9％ |
| Heavy hydrocarbon component (wt%) | 7.8％ | 4％ | 0％ | 2.4％ | 0％ | 88％ |
| Non-condensable gas (wt%) | 1.35％ | 0.13％ | 0％ | 61％ | 0％ | 0％ |
| Others (wt%) | 4.85％ | 55.37％ | 0％ | 6.6％ | 100％ | 3％ |
From the above table, 128122kg/h of propylene can be recovered in a 10-ten-thousand-ton propylene oxide-22.5-thousand-ton styrene/year plant.
Example two:
take the example of a device designed for a scale of 20 million tons of propylene oxide to 45 million tons of styrene per year.
The gas-phase product and the liquid-phase product from the propylene epoxidation reaction respectively enter a high-pressure propylene recovery tower T101 from different positions, the operating pressure of the high-pressure propylene recovery tower T101 is 1.78MPaG, the operating temperature of a tower kettle is 128 ℃, and the operating temperature of a tower top is 45 ℃. The product at the top of the high-pressure propylene recovery tower T101 is recovered propylene, the recovered propylene is removed from non-condensed steam by a non-condensed steam removal tower T104, and then the propylene product with a certain proportion is removed from a depropanizer T103 by an eleven delivery pipe 111, and the recovered propylene returns to a propylene epoxidation reactor by a twelve delivery pipe 112.
The propylene product at the top of the depropanizing tower T103 returns to the high-pressure propylene recovery tower T101 through a tenth conveying pipe 110, the hydrocarbon heavy component is discharged from the bottom of the depropanizing tower T103 through a ninth conveying pipe 109, the operating pressure of the depropanizing tower T103 is 1.72, the operating temperature of the bottom of the tower is 53 ℃, and the operating temperature of the top of the tower is 40 ℃.
The epoxidation reaction product containing a certain amount of propylene is discharged from the tower bottom of the high-pressure propylene recovery tower T101 and enters a flash water washing tank X101, a flash vapor phase enters a low-pressure propylene recovery tower T102, and a liquid phase is washed and also enters the low-pressure propylene recovery tower T102 from different positions. The product at the top of the low-pressure propylene recovery tower T102 is recovered propylene gas, the product at the bottom of the tower is a propylene epoxidation reaction product for removing propylene, and the operating pressure of the low-pressure propylene recovery tower is 0.23 MPaG. The product at the top of the low-pressure propylene recovery tower T102 is pressurized by a propylene compressor C101 and then is sent to the high-pressure propylene recovery tower T101 as a feed, and the outlet pressure of the propylene compressor C101 is 1.88 MPaG.
The composition parameters of the various streams are detailed in the following table:
| |
101 | 102 | 112 | 113 | 108 | 109 |
| Flow (kg/h) | 106399 | 409986 | 257773 | 510 | 257812 | 290 |
| Propylene (wt%) | 86％ | 40.5％ | 99.84％ | 30％ | 0％ | 9％ |
| Heavy hydrocarbon component (wt%) | 7.8％ | 4％ | 0％ | 2.4％ | 0％ | 88％ |
| Non-condensable gas (wt%) | 1.35％ | 0.13％ | 0％ | 61％ | 0％ | 0％ |
| Others (wt%) | 4.85％ | 55.37％ | 0％ | 6.6％ | 100％ | 3％ |
From the above table, 256273kg/h of propylene can be recovered in a 20-million ton propylene oxide-45-million ton styrene/year plant.
Example three:
take the example of a design scale plant of 13.5 million tons of propylene oxide to 30 million tons of styrene per year.
The gas-phase product and the liquid-phase product from the propylene epoxidation reaction respectively enter a high-pressure propylene recovery tower T101 from different positions, the operating pressure of the high-pressure propylene recovery tower T101 is 2MPaG, the operating temperature of a tower kettle is 131 ℃, and the operating temperature of a tower top is 45 ℃. The product at the top of the high-pressure propylene recovery tower T101 is recovered propylene, the recovered propylene is removed from non-condensed steam by a non-condensed steam removal tower T104, and then the propylene product with a certain proportion is removed from a depropanizer T103 by an eleven delivery pipe 111, and the recovered propylene returns to a propylene epoxidation reactor by a twelve delivery pipe 112.
The propylene product at the top of the depropanizing tower T103 returns to the high-pressure propylene recovery tower T101 through a tenth conveying pipe 110, the hydrocarbon heavy component is discharged from the bottom of the depropanizing tower T103 through a ninth conveying pipe 109, the operating pressure of the depropanizing tower T103 is 2.05, the operating temperature of the bottom of the depropanizing tower is 56 ℃, and the operating temperature of the top of the depropanizing tower is 41 ℃.
The epoxidation reaction product containing a certain amount of propylene is discharged from the tower bottom of the high-pressure propylene recovery tower T101 and enters a flash water washing tank X101, a flash vapor phase enters a low-pressure propylene recovery tower T102, and a liquid phase is washed and also enters the low-pressure propylene recovery tower T102 from different positions. The product at the top of the low-pressure propylene recovery tower T102 is recovered propylene gas, the product at the bottom of the tower is a propylene epoxidation reaction product for removing propylene, and the operating pressure of the low-pressure propylene recovery tower is 0.28 MPaG. The product at the top of the low-pressure propylene recovery tower T102 is pressurized by a propylene compressor C101 and then is sent to the high-pressure propylene recovery tower T101 as a feed, and the outlet pressure of the propylene compressor C101 is 2.1 MPaG.
The composition parameters of the various streams are detailed in the following table:
| |
101 | 102 | 112 | 113 | 108 | 109 |
| Flow (kg/h) | 74479 | 286990 | 180341 | 320 | 180608 | 200 |
| Propylene (wt%) | 86％ | 40.5％ | 99.90％ | 30％ | 0％ | 9％ |
| Heavy hydrocarbon component (wt%) | 7.8％ | 4％ | 0％ | 2.4％ | 0％ | 88％ |
| Non-condensable gas (wt%) | 1.35％ | 0.13％ | 0％ | 61％ | 0％ | 0％ |
| Others (wt%) | 4.85％ | 55.37％ | 0％ | 6.6％ | 100％ | 3％ |
From the above table, 179431kg/h of propylene can be recovered in a 13.5 ten thousand ton propylene oxide-30 ten thousand ton styrene/year plant.
Example four:
take an example of a design scale 5 million tons of propylene oxide to 11.25 million tons of styrene per year.
The gas-phase product and the liquid-phase product from the propylene epoxidation reaction respectively enter a high-pressure propylene recovery tower T101 from different positions, the operating pressure of the high-pressure propylene recovery tower T101 is 1.95MPaG, the operating temperature of a tower kettle is 128 ℃, and the operating temperature of a tower top is 45 ℃. The product at the top of the high-pressure propylene recovery tower T101 is recovered propylene, the recovered propylene is removed from non-condensed steam by a non-condensed steam removal tower T104, and then the propylene product with a certain proportion is removed from a depropanizer T103 by an eleven delivery pipe 111, and the recovered propylene returns to a propylene epoxidation reactor by a twelve delivery pipe 112.
The propylene product at the top of the depropanizing tower T103 returns to the high-pressure propylene recovery tower T101 through a tenth conveying pipe 110, the hydrocarbon heavy component is discharged from the bottom of the depropanizing tower T103 through a ninth conveying pipe 109, the operating pressure of the depropanizing tower T103 is 2.01, the operating temperature of the bottom of the tower is 55 ℃, and the operating temperature of the top of the tower is 41 ℃.
The epoxidation reaction product containing a certain amount of propylene is discharged from the tower bottom of the high-pressure propylene recovery tower T101 and enters a flash water washing tank X101, a flash vapor phase enters a low-pressure propylene recovery tower T102, and a liquid phase is washed and also enters the low-pressure propylene recovery tower T102 from different positions. The product at the top of the low-pressure propylene recovery tower T102 is recovered propylene gas, the product at the bottom of the tower is a propylene epoxidation reaction product for removing propylene, and the operating pressure of the low-pressure propylene recovery tower is 0.21 MPaG. The product at the top of the low-pressure propylene recovery tower T102 is pressurized by a propylene compressor C101 and then is sent to the high-pressure propylene recovery tower T101 as a feed, and the outlet pressure of the propylene compressor C101 is 2.05 MPaG.
The composition parameters of the various streams are detailed in the following table:
from the above table, 64365kg/h of propylene can be recovered in a 5-ten-thousand-ton propylene oxide-12.5-thousand-ton styrene/year apparatus.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. The utility model provides a propylene recovery unit of propylene oxide styrene coproduction system which characterized in that: comprises a high-pressure propylene recovery tower (T101), wherein the high-pressure propylene recovery tower (T101) is connected with an input pipeline of propylene epoxidation reaction products;
the top of the high-pressure propylene recovery tower (T101) is connected with a condenser (E101) through a fourteen conveying pipe (114), the bottom of the condenser (E101) is connected with a reflux tank (V101) through a fifteen conveying pipe (115), a gas phase outlet of the reflux tank (V101) is connected in series with a non-condensable gas removing tower (T104), the top of the non-condensable gas removing tower (T104) is connected with a thirteen conveying pipe (113), the bottom of the reflux tank (V101) is connected with an eleven conveying pipe (111) and a twelve conveying pipe (112), and the eleven conveying pipe (111) is connected with a depropanizing tower (T103);
the top of the depropanizing tower (T103) is connected with a high-pressure propylene recovery tower (T101) through a tenth conveying pipe (110), and the bottom of the tower kettle of the depropanizing tower (T103) is connected with a ninth conveying pipe (109);
the high-pressure propylene recovery tower (T101) tower bottom links to each other through third conveyer pipe (103) with flash water washing jar (X101), the top and low pressure propylene recovery tower (T102) of flash water washing jar (X101) link to each other through fourth conveyer pipe (104), and the bottom and the low pressure propylene recovery tower (T102) of flash water washing jar (X101) link to each other through fifth conveyer pipe (105), the top of the tower of low pressure propylene recovery tower (T102) links to each other with high-pressure propylene recovery tower (T101), the tower bottom of low pressure propylene recovery tower (T102) even has eighth conveyer pipe (108).
2. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 1, wherein: the feed line for the epoxidation reaction product of propylene comprises a first feed line (101) and a second feed line (102), and the first feed line (101) and the second feed line (102) are connected to different tray positions of the high-pressure propylene recovery column (T101).
3. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 1, wherein: the fourth duct (104) is connected to the upper tray of the low-pressure propylene recovery column (T102), and the fifth duct (105) is connected to the top of the low-pressure propylene recovery column (T102).
4. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 1, wherein: the connecting pipeline between the tower top of the low-pressure propylene recovery tower (T102) and the high-pressure propylene recovery tower (T101) is provided with a propylene compressor, the propylene compressor is connected with the low-pressure propylene recovery tower (T102) through a sixth conveying pipe (106) and is connected with the high-pressure propylene recovery tower (T101) through a seventh conveying pipe (107).
5. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 1, wherein: the operating pressure of the high-pressure propylene recovery column (T101) is 1.6 to 2.2MPaG in terms of gauge pressure, the operating pressure of the low-pressure propylene recovery column (T102) is 0.1 to 0.4MPaG in terms of gauge pressure, and the operating pressure of the depropanizer column (T103) is 1.5 to 2.1MPaG in terms of gauge pressure.
6. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 4, wherein: the outlet pressure of the propylene compressor is 1.7-2.3 MPaG in gauge pressure.
7. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 1, wherein: the operation temperature of the tower kettle of the high-pressure propylene recovery tower (T101) is 100-140 ℃, and the operation temperature of the tower top of the high-pressure propylene recovery tower (T101) is 30-50 ℃.
8. The propylene recovery device of the co-production system of propylene oxide and styrene as claimed in claim 1, wherein: the tower kettle operation temperature of the depropanizing tower (T103) is 50-60 ℃, and the tower top operation temperature of the depropanizing tower (T103) is 30-50 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120673135.XU CN215162247U (en) | 2021-04-01 | 2021-04-01 | Propylene recovery device of epoxypropane styrene coproduction system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120673135.XU CN215162247U (en) | 2021-04-01 | 2021-04-01 | Propylene recovery device of epoxypropane styrene coproduction system |
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| Publication Number | Publication Date |
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| CN215162247U true CN215162247U (en) | 2021-12-14 |
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| CN202120673135.XU Active CN215162247U (en) | 2021-04-01 | 2021-04-01 | Propylene recovery device of epoxypropane styrene coproduction system |
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| CN (1) | CN215162247U (en) |
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