CN104128063A - Device and method for recovery of olefin monomer in tail gas from polypropylene production - Google Patents
Device and method for recovery of olefin monomer in tail gas from polypropylene production Download PDFInfo
- Publication number
- CN104128063A CN104128063A CN201410367808.3A CN201410367808A CN104128063A CN 104128063 A CN104128063 A CN 104128063A CN 201410367808 A CN201410367808 A CN 201410367808A CN 104128063 A CN104128063 A CN 104128063A
- Authority
- CN
- China
- Prior art keywords
- olefinic monomer
- tail gas
- propylene
- gas
- recovery tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The invention discloses a device and method for recovery of olefin monomers in tail gas from polypropylene production. The device comprises an olefin monomer recovery tower and a hydrophobic aggregation packing assembly; the olefin monomer recovery tower is provided with an exhaust inlet, an exhaust outlet and an olefin monomer outlet; the exhaust outlet is higher than the exhaust inlet; the exhaust inlet is higher than the olefin monomer outlet; the hydrophobic aggregation packing assembly is arranged in the inner cavity of the olefin monomer recovery tower, between the exhaust inlet and exhaust outlet, and near the exhaust outlet. Through arrangement of the hydrophobic aggregation packing assembly in a traditional olefin monomer recovery device, the recovery device of the invention increases the coalescence opportunity of tiny propylene droplets, reduces the opportunity of entraining propylene droplets by ethylene, increases the opportunity of ethylene dissolving in propylene, improves the efficiency of ethylene absorption by propylene in recovery device, not only reduces the treatment cost and energy consumption, but also simplifies the process, and is easy for scale application.
Description
Technical field
The present invention relates to technical field of chemical engineering, produce from polypropylene the method and apparatus that reclaims olefinic monomer tail gas in particular to a kind of.
Background technology
Polypropylene is second-biggest-in-the-world synthetic resin kind.Polypropylene has good mechanical performance, heat resistance, and electrical insulation properties,, there is not chemical action with most chemicals in chemical stability; On the other hand, polypropylene has advantages of the processing and forming of being easy to.Its shortcoming is that low-temperature impact resistance is poor, and more aging, dyeability is poor, is a kind of general-purpose plastics.It is water insoluble, does not also absorb water, and can in water, boil and boil, and can at 130 DEG C, sterilize.The premium properties of its product makes it be used widely in industries such as packaging, fiber, electronic apparatus, auto parts and components, commodity and medicine equipments.
The Eleventh Five-Year Plan period, the fast-developing impetus that domestic oil refining, ethylene industry keep, drives polypropylene industrial all the time in rising situation.The Eleventh Five-Year Plan period, the fast-developing impetus that domestic oil refining, ethylene industry keep, drives polypropylene industrial all the time in rising situation.2006, the polypropylene production capacity of China was 5,780,000 tons/year, and to 2010 the end of the year China polyethylene production capacity reached 1,112 ten thousand tons/year, production capacity is compared the Eleventh Five-Year Plan initial stage and has been increased by 5,680,000 tons/year, production capacity growth rate is apparently higher than polyethylene.Polypropylene production capacity increases comparatively stable, and the main more diversification of ethene because compare in the source of polypropylene upstream propylene comprises that the projects such as refinery's polypropylene, MTP, MTO and preparing propylene by dehydrogenating propane build up and put on market one after another in recent years.From in recent years, it is mainly at 2007,2009 and 2010 that the polypropylene production capacity of China is thrown in.This production capacity in 3 years growth has reached 4,690,000 tons.
Polymarization method for prodcing polyacrylates has gas-liquid combined method, vapor phase method, liquid phase noumenal method, solvent method (slurry process), and wherein, solvent method, because production process is more complicated, also will reclaim the reasons such as solvent, is progressively eliminated.At present, vapor phase method is occupied an leading position, but, this technique point to from Gao Rong low while melting the fingering row conversion trade mark, the discharge gas of reactor enters discharge air cooling condensation reclaiming system, discharge gas first enter discharge gas condenser circulating cooling water condensation laggard enter condensate liquid knockout drum.Fixed gas is disposed to battery limit (BL) outer fuel pipe network, and the propylene liguid under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
Above-mentioned polypropylene exists a large amount of tail gas to need harmless treatment in process of production, and traditional technique exists following shortcoming: (1) whole removal process technological process is long.Because the quality percentage composition of olefin component in tail gas is lower than 80%, the disposal ability of existing equipment is limited, can only add the size of large equipment, causes the waste of equipment investment, causes separation costs corresponding higher.(2) due to ethylene component, to form liquid temperature lower, causes gaseous ethylene to carry propylene liguid secretly to enter flare system and cause the loss of olefin component.
While polypropylene being switched to the trade mark due to the existence of traditional separation method, in tail gas, olefinic monomer is difficult to the shortcoming fully reclaiming, need to develop one efficiently, novel process for separating and recovering cheaply, reduce recovery cost, reach the object of effective recovery alkene.
Summary of the invention
The present invention aims to provide a kind of equipment and method that reclaims olefinic monomer from polypropylene production tail gas, efficiently and economically to produce tail gas and to reclaim olefinic monomer from polypropylene.
To achieve these goals, according to an aspect of the present invention, provide a kind of and produced from polypropylene the equipment that reclaims olefinic monomer tail gas, this equipment comprises: olefinic monomer recovery tower and hydrophobicity coalescence filler assembly; On olefinic monomer recovery tower, have gas inlet, tail gas outlet and olefinic monomer outlet, tail gas exports higher than gas inlet, and gas inlet exports higher than olefinic monomer; Hydrophobicity coalescence filler assembly, is arranged in the inner chamber of olefinic monomer recovery tower, and between gas inlet and tail gas outlet, near tail gas, outlet arranges.
Further, the said equipment also comprises condensing unit, and condensing unit is arranged in olefinic monomer recovery tower inner chamber, and is arranged between gas inlet and hydrophobicity coalescence filler assembly.
Further, the said equipment also comprises gas-liquid separation device, gas-liquid separation device is arranged in olefinic monomer recovery tower inner chamber, and is arranged between gas inlet and condensing unit, and preferably gas-liquid separation device is to separate the gas-liquid separation chamber that olefinic monomer recovery tower inner chamber forms.
Further, above-mentioned hydrophobicity coalescence filler assembly is structured packing assembly or dumped packing assembly, and preferably structured packing assembly comprises multiple structured packing plates that be arranged in parallel, and the upright projection of each structured packing plate is covered with the cross section of olefinic monomer recovery tower.
Further, the form of above-mentioned structured packing plate is ripple net or corrugated plating.
Further, in above-mentioned structured packing assembly, each structured packing plate has the inclination angle of 30 °～60 ° with respect to vertical direction, and the spacing of preferred adjacent structured packing plate is 5～50cm.
Further, in above-mentioned hydrophobicity coalescence filler assembly, filler is selected from any in polytetrafluoroethylene (PTFE), polyethylene, polypropylene, polyvinyl chloride, polystyrene or polyester.
Further, above-mentioned condensing unit comprises the heat exchanger tube that is arranged on olefinic monomer recovery tower inside, and is connected with heat exchanger tube and extends to condensate liquid entrance and the condensate outlet of olefinic monomer recovery tower outside.
According to a further aspect in the invention, provide a kind of and produced from polypropylene the method that reclaims olefinic monomer tail gas, the method comprises: from the gas inlet of the olefinic monomer recovery tower of above-mentioned any equipment, polypropylene is produced to tail gas and is passed into the inside of olefinic monomer recovery tower, through hydrophobicity coalescence filler assembly coalescence, form liquid olefin monomer; From olefinic monomer outlet withdrawal liquid olefinic monomer.
Further, above-mentioned polypropylene is produced tail gas taking pressure as 0.1～4.0MPaG, and apparent velocity is that 0.01～20cm/s passes into olefinic monomer recovery tower.
Further, in the time being provided with condensing unit in olefinic monomer recovery tower, in condensing unit, condensation temperature is-30 DEG C～30 DEG C.
Apply technical scheme of the present invention, by the inside of the olefinic monomer reclaimer traditional, hydrophobicity coalescence filler assembly is set, the tail gas that makes to comprise propylene drop is during through hydrophobicity coalescence filler assembly, increase the chance of propylene fine droplet coalescence, reduce the chance that ethylene gas is carried propylene drop secretly, meanwhile, increase the chance of propylene dissolve ethylene, improved the efficiency of propylene absorption ethene in reclaimer.Above-mentioned reclaimer of the present invention, had both reduced the processing cost and the energy consumption that from tail gas, reclaim olefinic monomer, had simplified again technical process, was easy to scale application.
Brief description of the drawings
The Figure of description that forms the application's a part is used to provide a further understanding of the present invention, and schematic description and description of the present invention is used for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 shows the equipment that olefinic monomer is provided in the tail gas producing from produce polyacrylic process providing in a kind of typical embodiment of the present invention.
Detailed description of the invention
It should be noted that, in the situation that not conflicting, the feature in embodiment and embodiment in the application can combine mutually.Describe below with reference to the accompanying drawings and in conjunction with the embodiments the present invention in detail.
Mention as background technology part, traditional separation method exists olefinic monomer in tail gas to be difficult to the shortcoming fully reclaiming, in order to improve above-mentioned shortcoming, in a kind of typical embodiment of the present invention, provide a kind of and produced from polypropylene the equipment that reclaims olefinic monomer tail gas, this equipment comprises: olefinic monomer recovery tower and hydrophobicity coalescence filler assembly 4.On olefinic monomer recovery tower, have gas inlet 1, tail gas outlet 2 and olefinic monomer outlet 3, described tail gas outlet 2 is higher than described gas inlet 1; Described gas inlet 1 is higher than described olefinic monomer outlet 3; Hydrophobicity coalescence filler assembly 4, is arranged on the inner chamber top of described olefinic monomer recovery tower, between described gas inlet 1 and described tail gas outlet 2, and arranges near described tail gas outlet 2.
The said equipment of the present invention arranges hydrophobicity coalescence filler assembly 4 by the inside of the olefinic monomer reclaimer traditional, the tail gas that makes to comprise propylene drop is during through hydrophobicity coalescence filler assembly 4, increase the chance of propylene fine droplet coalescence, reduce the chance that ethylene gas is carried propylene drop secretly, simultaneously, increase the chance of propylene dissolve ethylene, improved the efficiency of propylene absorption ethene in reclaimer.Above-mentioned reclaimer of the present invention is compared traditional separation reclaimer, has both reduced the processing cost and the energy consumption that reclaim olefinic monomer in tail gas, has simplified again technical process, is easy to scale application.
In the said equipment of the present invention, traditional olefinic monomer recovery tower can be realized cooling of tail gas, makes the propylene in tail gas be condensed into liquid, such as, plate type heat exchanger, finned heat exchanger etc.For the temperature of further fast reducing tail gas, promote the condensation of propylene in tail gas, in a kind of preferred embodiment of the present invention, the said equipment also comprises condensing unit 5, and be arranged between the gas inlet 1 and hydrophobicity coalescence filler assembly 4 of olefinic monomer recovery tower inside, make the propylene monomer in the condensed tail gas of condensing unit 5 be condensed into fine droplet, thereby by above-mentioned hydrophobicity coalescence filler assembly 4 of the present invention, increase coalescence chance, reduce gas carrying secretly propylene monomer.
In the another kind of preferred embodiment of the present invention, in the said equipment, also comprise and be positioned at olefinic monomer recovery tower inside, and be arranged on the gas-liquid separation device 6 between gas inlet 1 and condensing unit 5, be condensed into liquid for receiving through condensing unit 5, and become drop to return fallen propylene drop or be dissolved with the propylene drop of ethene through the further coalescence of hydrophobicity gathering board assembly, to further collect olefinic monomers from olefinic monomer outlet 3.Further preferred described gas-liquid separation device 6 is exactly to separate the gas-liquid separation chamber that above-mentioned olefinic monomer recovery tower inner chamber forms.
In the said equipment of the present invention, above-mentioned hydrophobicity coalescence filler assembly 4 is to utilize its hydrophobicity by the propylene fine droplet coalescence in gas phase, thereby be convenient to propylene liguid to reclaim, simultaneously, hydrophobicity coalescence filler assembly 4 provides large surface for propylene liguid, propylene liguid can be sprawled in the above, and then can fully absorb the ethene in gas phase.Therefore, the form of above-mentioned hydrophobicity coalescence filler be there is no to particular/special requirement, as long as can function as described above.
In a kind of preferred embodiment of the present invention, the form of above-mentioned hydrophobicity coalescence filler assembly 4 is structured packing assembly or dumped packing assembly, and dumped packing assembly is made up of one or more different dumped packings.Wherein, be applicable to dumped packing of the present invention and comprise one or more in Raschig ring, Pall ring, Intalox saddle, cascade ring, Intelux filling, Dixon ring, saddle type net.While adopting above-mentioned dumped packing, gas and propylene liguid time of contact and the contact area in equipment be can increase, the coalescence of propylene liguid and the dissolving to ethene in gas are convenient to.
In the time that the form of above-mentioned hydrophobicity coalescence filler assembly 4 is structured packing assembly, preferred above-mentioned structured packing assembly comprises multiple structured packing plates that be arranged in parallel, and the upright projection of each structured packing plate is covered with the cross section of olefinic monomer recovery tower.Adopt structured packing plate to be more conducive to propylene drop coalescence, and arrange conveniently.In the another kind of preferred embodiment of the present invention, the form of above-mentioned structured packing plate is ripple net or corrugated plating, and the hole of ripple net is large compared with corrugated plating hole, but can arrange with the form of plate, and it is more convenient to operate.Meanwhile, also can increase the contact area of gas and propylene liguid, promote the dissolving of ethene in propylene liguid in gas.
In a kind of preferred embodiment of the present invention, in above-mentioned structured packing assembly, each structured packing plate has the inclination angle of 30 °～60 ° with respect to exhaust gas flow direction, and the spacing of preferred adjacent structured packing plate is 5～50cm.Above-mentioned structured packing plate is set at a certain angle, can promotes mixing of gas and propylene liguid, increase time of contact and contact area, promote the absorption of propylene liguid to ethene in tail gas.In the time that structured packing plate is set to be the inclination angle of 30 °～60 ° with respect to exhaust gas flow mode, more can promote the coalescence of propylene liguid, meanwhile, also higher to the absorption efficiency of ethene in tail gas.In like manner, in the time that structured packing plate is set, between adjacent structured packing plate, keep also fully contacting of favourable gas and liquid of certain spacing, promote the separation of olefinic monomer from tail gas.In the time that spacing is 5～50cm, separating effect is better.
In above-mentioned hydrophobicity coalescence filler assembly 4 of the present invention, the material of hydrophobicity coalescence filler assembly be there is no to particular/special requirement, meet hydrophobicity, and do not react with olefines material.For example, hydrophobic polytetrafluoroethylene (PTFE), polyethylene, polypropylene, polyvinyl chloride, polystyrene or polyester are all applicable to the present invention.
As long as can play the tail gas effect that cools at above-mentioned condensing unit 5 of the present invention, the concrete configuration of this condensing unit 5 be there is no to particular/special requirement.In another preferred embodiment of the present invention, above-mentioned condensing unit 5 comprises the heat exchanger tube that is arranged on olefinic monomer recovery tower inside, and is connected with heat exchanger tube and extends to condensate liquid entrance and the condensate outlet of olefinic monomer recovery tower outside.There is the condensing unit 5 of said structure, have and can fully the propylene in tail gas be condensed into propylene liguid, be beneficial to the coalescence of follow-up propylene liguid and further the ethene in tail gas dissolved, and then reducing to a greater degree the content of ethene in tail gas.Meanwhile, in above-mentioned heat exchanger tube, can use liquefied ammonia, chilled water or pure water etc., the water of the preferred convenient sources of the present invention is lowered the temperature, and water can also recycle.
In the another kind of typical embodiment of the present invention, also provide a kind of and produced from polypropylene the method that reclaims olefinic monomer tail gas, method comprises: the gas inlet 1 of the olefinic monomer recovery tower from above-mentioned any equipment, polypropylene is produced to tail gas and passed into the inside of olefinic monomer recovery tower, forming liquid olefin monomers through hydrophobicity coalescence filler assembly 4 coalescences; Then the liquid olefin monomer reclaiming through 43 coalescences of hydrophobicity coalescence filler assembly from olefinic monomer outlet 35.
Said method of the present invention by increasing the coalescence chance of propylene liguid, has reduced ethylene gas and has carried propylene drop secretly in olefinic monomer recovery tower, meanwhile, improves the efficiency of the propylene absorption ethene in tower.The method is different from traditional separating technology, has reduced the processing cost that reclaims olefinic monomer in tail gas, has reduced the energy consumption separating, and has simplified technical process.
In said method of the present invention, the tail gas pressure or the flow velocity that pass into be there is no to particular/special requirement, conventional parameter setting is carried out to suitable improvement and can apply to the present invention.In a kind of preferred embodiment of the present invention, polypropylene is produced to tail gas taking pressure as 0.1～4.0MPaG, apparent velocity is that 0.01～20cm/s passes into olefinic monomer recovery tower.When by passing into the pressure of tail gas and flow control in above-mentioned scope time, be both conducive to separate efficiently the olefin monomer in above-mentioned tail gas, can realize again the maximization of the utilization to the said equipment, reduce energy consumption.
In another preferred embodiment of the present invention, when tail gas passes through above-mentioned condensing unit 5, in condensing unit 5, condensation temperature is-30 to+30 degrees Celsius, in this temperature range, can more rapidly more propylene in tail gas be condensed into propylene liguid, be beneficial to the separation of propylene liguid and follow-up ethene.
Further illustrate below in conjunction with specific embodiments beneficial effect of the present invention.
It should be noted that, in the following example, equipment used is olefinic monomer recovery tower as shown in Figure 1, arranges respectively: 1 gas inlet at the upper and lower two ends of olefinic monomer recovery tower; 2 tail gas outlets; 3 olefinic monomer outlets; 4 hydrophobicity coalescence filler assemblies; 5 condensing units; 6 gas-liquid separation chamber; 51 condensate liquid imports; 52 condensate outlets.
This equipment is that the stainless head tower of the high 3m of being of 20cm is as reclaiming olefinic monomer recovery tower main body in tail gas in polypropylene production process with internal diameter, bottom enters gas-liquid separation chamber from tail gas import, propylene heat exchanger tube is installed on top in gas-liquid separation chamber, and hydrophobicity coalescence device is equipped with on top.
Wherein, the detection method of olefinic monomer is used gas chromatography (Hewlett-Packard's 6890 gas chromatographs).
In the following example, the separative efficiency of alkene is by calculating in undefined mode:
Definition: separation of olefins efficiency=(reclaiming the exit concentration * outlet exhaust gas volumes of initial concentration × import exhaust gas volumes-recovery olefinic monomer of olefinic monomer in tail gas)/(reclaiming initial concentration × import exhaust gas volumes of olefinic monomer in tail gas) × 100%
Embodiment 1
In embodiment 1, adopt polyethylene hydrophobicity coalescence device, wherein, the inclination angle that arranges of each gathering board is 45 °, and spacing is 25cm.Passing into from the tail gas import of tail gas knockout tower the density of propylene producing polypropylene production process is 0.135wt%, ethylene concentration is the tail gas of 0.168wt%, gas superficial flow velocity is that 1cm/s passes into (40 DEG C of exhaust temperatures, pressure 2.0MPaG), first discharge gas enter tail gas knockout, then use recirculated cooling water from circulating water intake (25 DEG C of circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (circulating water temperature-10 DEG C, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in hydrophobic material polytetrafluoroethylene (PTFE) Raschig ring surface coalescence, and after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.From tail gas outlet, fixed gas is disposed to fuel pipe network, the propylene liguid that condensation is got off and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 0.110wt%; The concentration of ethene is 0.126wt%.As calculated, the rate of recovery of propylene is 81%, the rate of recovery 75% of ethene.
Embodiment 2
In embodiment 2, adopt hydrophobic polypropylene coalescence device, wherein, the inclination angle that arranges of each gathering board is 60 °, and spacing is 50cm.Add from tail gas import the density of propylene 3.10wt% producing polypropylene production process, ethylene concentration is the tail gas of 4.10wt%, gas superficial flow velocity 4cm/s passes into (43 DEG C of exhaust temperatures, pressure 0.1MPaG), first discharge gas enter tail gas knockout, then use recirculated cooling water from circulating water intake (25 DEG C of circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (circulating frozen coolant-temperature gage-30 DEG C, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in the surperficial coalescence of hydrophobic material (polytetrafluoroethylene (PTFE) saddle type net), and after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.Tail gas outlet fixed gas is disposed to fuel pipe network, and the liquid propylene under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 2.20wt%; The concentration of ethene is 1.68wt%.The rate of recovery of propylene is 71%, the rate of recovery 41% of ethene.
Embodiment 3
In embodiment 3, adopt polystyrene hydrophobicity coalescence device, wherein, the inclination angle that arranges of each gathering board is 30 °, and spacing is 5cm.Adding the density of propylene polypropylene production process from the tail gas import described in EXAMPLE l is 0.0100wt%, ethylene concentration is the tail gas of 0.0130wt%, gas superficial flow velocity 3cm/s passes into (46 DEG C of exhaust temperatures, pressure 4.0MPaG), first discharge gas enter tail gas knockout, then use recirculated cooling water from circulating water intake (20 DEG C of circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (30 DEG C of circulating water temperatures, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in the surperficial coalescence of hydrophobic material (polytetrafluoroethylene (PTFE) ripple net is filled angle 30 and spent), and after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.Tail gas outlet fixed gas is disposed to fuel pipe network, and the propylene liguid under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 0.00840wt%; The concentration of ethene is 0.00767wt%.The rate of recovery of propylene is 84%, the rate of recovery 59% of ethene.
Embodiment 4
In embodiment 4, adopt polytetrafluoroethylene (PTFE) hydrophobicity coalescence device, wherein, in coalescence device, the inclination angle that arranges of each gathering board is 75 °, and spacing is 60cm.Adding the density of propylene polypropylene production process from the tail gas import described in EXAMPLE l is 0.200wt%, ethylene concentration is the tail gas of 0.300wt%, gas superficial flow velocity 3cm/s passes into (40 DEG C of exhaust temperatures, pressure 2.0MPaG), first discharge gas enter tail gas knockout, then use recirculated cooling water from 25 DEG C of circulating water intake circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (30 DEG C of circulating water temperatures, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in the surperficial coalescence of hydrophobic material (polytetrafluoroethylene (PTFE) ripple net is filled angle 60 and spent), and after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.Tail gas outlet fixed gas is disposed to fuel pipe network, and the propylene liguid under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 0.0700wt%; The concentration of ethene is 0.0960wt%.The rate of recovery of propylene is 35%, the rate of recovery 32% of ethene.
Embodiment 5
In embodiment 5, adopt polyvinyl chloride hydrophobicity coalescence device, wherein, the inclination angle that arranges of each gathering board of coalescence device is 35 °, and spacing is 20cm.Adding the density of propylene polypropylene production process from the tail gas import 4 described in EXAMPLE l is 0.150wt%, ethylene concentration is the tail gas of 0.170wt%, gas superficial flow velocity 0.1cm/s passes into (38 DEG C of exhaust temperatures, pressure 2.5MPaG), first discharge gas enter tail gas knockout 1, then use recirculated cooling water from circulating water intake (25 DEG C of circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (29 DEG C of circulating water temperatures, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in hydrophobic material (the board-like structured packing of polytetrafluoroethylene (PTFE), filling angle 30 spends, distance between plates 5cm) surperficial coalescence, after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.Tail gas outlet fixed gas is disposed to fuel pipe network, and the propylene liguid under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 0.137wt%; The concentration of ethene is 0.111wt%.The rate of recovery of propylene is 91%, the rate of recovery 65% of ethene.
Embodiment 6
In embodiment 6, adopt polyvinyl chloride hydrophobicity coalescence device, wherein, the inclination angle that arranges of each gathering board of coalescence device is 55 °, and spacing is 40cm.Adding the density of propylene polypropylene production process from the tail gas import 4 described in EXAMPLE l is 0.400wt%, ethylene concentration is the tail gas of 0.500wt%, gas superficial flow velocity 20cm/s passes into (38 DEG C of exhaust temperatures, pressure 1.0MPaG), first discharge gas enter tail gas knockout 1, then use recirculated cooling water from circulating water intake (25 DEG C of circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (29 DEG C of circulating water temperatures, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in hydrophobic material (the board-like structured packing of polyethylene, filling angle 60 spends, distance between plates 10cm) surperficial coalescence, after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.Tail gas outlet fixed gas is disposed to fuel pipe network, and the propylene liguid under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 0.296wt%; The concentration of ethene is 0.215wt%.The rate of recovery of propylene is 74%, the rate of recovery 43% of ethene.
Embodiment 7
In embodiment 7, adopt polyvinyl chloride hydrophobicity coalescence device, wherein, the inclination angle that arranges of each gathering board of coalescence device is 40 °, and spacing is 10cm.Adding the density of propylene polypropylene production process from the tail gas import 4 described in EXAMPLE l is 0.120wt%, ethylene concentration is the tail gas of 0.170wt%, gas superficial flow velocity 2cm/s passes into (40 DEG C of exhaust temperatures, pressure 2.4MPaG), first discharge gas enter tail gas knockout 1, then use recirculated cooling water from circulating water intake (25 DEG C of circulating water temperatures, pressure 0.4MPaG) enter after tail gas condenser, eject condensation tail gas from circulating water outlet (30 DEG C of circulating water temperatures, pressure 0.3MPaG).Finally, tail gas enters in tail gas coalescence device, and propylene drop is in the surperficial coalescence of hydrophobic material (polyethylene Pall ring), and after propylene liguid fully contacts with gaseous ethylene simultaneously, ethene absorbs and enters in propylene liguid.Tail gas outlet fixed gas is disposed to fuel pipe network, and the propylene liguid under condensation and mixture of ethylene are transported to defective propylene tank outside battery limit (BL).
After testing, in the propylene liguid that recovery obtains and the mixture of ethene, the concentration of propylene is 0.0916wt%; The concentration of ethene is 0.0969wt%.The rate of recovery of propylene is 76%, the rate of recovery 57% of ethene.
From above description, can find out, the above embodiments of the present invention have realized following technique effect: by the inside of the olefinic monomer reclaimer traditional, hydrophobicity coalescence filler assembly is set, the tail gas that makes to comprise propylene drop is during through hydrophobicity coalescence filler assembly, increase the chance of propylene fine droplet coalescence, reduce the chance that ethylene gas is carried propylene drop secretly, meanwhile, improved the efficiency of propylene absorption ethene in reclaimer.Above-mentioned reclaimer of the present invention is different from traditional separation reclaimer, has both reduced the processing cost and the energy consumption that reclaim olefinic monomer in tail gas, has simplified again technical process, is easy to scale application.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment of doing, be equal to replacement, improvement etc., within all should being included in protection scope of the present invention.
Claims (11)
1. produce from polypropylene an equipment that reclaims olefinic monomer tail gas, it is characterized in that, described equipment comprises:
Olefinic monomer recovery tower, has gas inlet (1), tail gas outlet (2) and olefinic monomer outlet (3) on it, described tail gas outlet (2) is higher than described gas inlet (1); Described gas inlet (1) exports (3) higher than described olefinic monomer;
Hydrophobicity coalescence filler assembly (4), is arranged in the inner chamber of described olefinic monomer recovery tower, is positioned between described gas inlet (1) and described tail gas outlet (2), arranges near described tail gas outlet (2).
2. equipment according to claim 1, it is characterized in that, described equipment also comprises condensing unit (5), described condensing unit (5) is arranged in described olefinic monomer recovery tower inner chamber, and is arranged between described gas inlet (1) and described hydrophobicity coalescence filler assembly (4).
3. equipment according to claim 2, it is characterized in that, described equipment also comprises gas-liquid separation device (6), described gas-liquid separation device (6) is arranged in described olefinic monomer recovery tower inner chamber, and be arranged between described gas inlet (1) and described condensing unit (5) gas-liquid separation chamber that preferred described gas-liquid separation device (6) forms for separating described olefinic monomer recovery tower inner chamber.
4. equipment according to claim 1, it is characterized in that, described hydrophobicity coalescence filler assembly (4) is structured packing assembly or dumped packing assembly, preferred described structured packing assembly comprises multiple structured packing plates that be arranged in parallel, and the upright projection of each described structured packing plate is covered with the cross section of described olefinic monomer recovery tower.
5. equipment according to claim 4, is characterized in that, the version of described structured packing plate is ripple net or corrugated plating.
6. according to the equipment described in claim 4 or 5, it is characterized in that, in described structured packing assembly, each described structured packing plate has the inclination angle of 30 °～60 ° with respect to vertical direction, and preferably the spacing of adjacent described structured packing plate is 5～50cm.
7. equipment according to claim 1, is characterized in that, described hydrophobicity coalescence filler assembly (4) is selected from any in polytetrafluoroethylene (PTFE), polyethylene, polypropylene, polyvinyl chloride, polystyrene or polyester.
8. according to the equipment described in claim 2 or 3, it is characterized in that, described condensing unit (5) comprises the heat exchanger tube that is arranged on described olefinic monomer recovery tower inside, and is connected with described heat exchanger tube and extends to condensate liquid entrance (51) and the condensate outlet (52) of olefinic monomer recovery tower outside.
9. produce from polypropylene a method that reclaims olefinic monomer tail gas, it is characterized in that, described method comprises:
The gas inlet (1) of the olefinic monomer recovery tower in the equipment from claim 1 to 8 described in any one, polypropylene is produced to tail gas and is passed into the inside of described olefinic monomer recovery tower, through described hydrophobicity coalescence filler assembly (4) coalescence, form liquid olefin monomer;
Reclaim described liquid olefin monomer from olefinic monomer outlet (3).
10. method according to claim 9, is characterized in that, described polypropylene is produced tail gas taking pressure as 0.1～4.0MPaG, and apparent velocity is that 0.01～20cm/s passes into described olefinic monomer recovery tower.
11. methods according to claim 10, is characterized in that, in the time being provided with condensing unit in described olefinic monomer recovery tower, in described condensing unit, condensation temperature is-30 DEG C～30 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410367808.3A CN104128063B (en) | 2014-07-29 | 2014-07-29 | Device and method for recovery of olefin monomer in tail gas from polypropylene production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410367808.3A CN104128063B (en) | 2014-07-29 | 2014-07-29 | Device and method for recovery of olefin monomer in tail gas from polypropylene production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104128063A true CN104128063A (en) | 2014-11-05 |
| CN104128063B CN104128063B (en) | 2017-01-18 |
Family
ID=51801074
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410367808.3A Active CN104128063B (en) | 2014-07-29 | 2014-07-29 | Device and method for recovery of olefin monomer in tail gas from polypropylene production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104128063B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108778486A (en) * | 2016-03-10 | 2018-11-09 | 林德股份公司 | Device and method for being fitted into the packing box of structured packing in the container of mass transfer column |
| CN109312016A (en) * | 2016-11-17 | 2019-02-05 | Lg化学株式会社 | Olefinic monomer recyclable device |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006281045A (en) * | 2005-03-31 | 2006-10-19 | Matsushita Electric Ind Co Ltd | Gas recovery apparatus |
| CN101670225B (en) * | 2009-10-19 | 2012-01-18 | 浙江赞宇科技股份有限公司 | Sulfonated tail gas cycle-absorption method and cycle-absorption system |
| CN201899968U (en) * | 2010-10-14 | 2011-07-20 | 中国石油化工股份有限公司 | Oil gas recovery device combining condensation method with adsorption method |
-
2014
- 2014-07-29 CN CN201410367808.3A patent/CN104128063B/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108778486A (en) * | 2016-03-10 | 2018-11-09 | 林德股份公司 | Device and method for being fitted into the packing box of structured packing in the container of mass transfer column |
| CN109312016A (en) * | 2016-11-17 | 2019-02-05 | Lg化学株式会社 | Olefinic monomer recyclable device |
| CN109312016B (en) * | 2016-11-17 | 2021-05-18 | Lg化学株式会社 | Olefin monomer recovery device |
| US11478725B2 (en) | 2016-11-17 | 2022-10-25 | Lg Chem, Ltd. | Olefinic monomer recovery apparatus |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104128063B (en) | 2017-01-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104923029B (en) | The recovery method of vapor phase method polyolefin emission | |
| CN103044257B (en) | Terylene waste material produces alcoholysis method and the apparatus system of dioctyl terephthalate | |
| CN102548653A (en) | Process for producing steam using heat recovered from a polymerization reaction | |
| CN102389643B (en) | Exhaust gas recycling method and device for olefin polymer production | |
| CN116917101A (en) | Method for pyrolysis of mixed plastic waste containing PVC | |
| CN212833550U (en) | Propane dehydrogenation product separation device | |
| CN203648114U (en) | Cumene recovery device | |
| CN104128063A (en) | Device and method for recovery of olefin monomer in tail gas from polypropylene production | |
| CN104185495B (en) | Process for recovering hydrocarbons from polyolefin plants and apparatus suitable for purpose | |
| CN103030494B (en) | Absorption and hydration coupling device and method for separating ethylene and ethane in catalytic cracking dry gas or ethylene pyrolysis gas | |
| CN211339346U (en) | Energy-saving separation system for four components of carbon behind ether | |
| CN106478363A (en) | The technique of recycling design and monomer in Butyl Rubber | |
| CN105585417A (en) | Method for producing ethyl benzene from exhaust gas of polyethylene device | |
| CN203947052U (en) | The device of a kind of refining trioxymethylene and recovery benzene | |
| CN105964004A (en) | Device for self-heat extracting to flash evaporate sulfuric acid alkylation reaction product | |
| CN206359443U (en) | A kind of methyl tertiary butyl ether(MTBE) mixed solvent separator | |
| CN203007176U (en) | Alcoholysis device system for preparing dioctyl terephthalate from Dacron wastes | |
| CN213760550U (en) | Two-tower double-heat-pump integrated 1-butene refining energy-saving device | |
| CN104803833A (en) | Liquid phase temperature swing adsorption separating dehydration method for preparing polymethoxydialkyl ether | |
| CN212025224U (en) | Fine separation device for olefin catalytic cracking products | |
| CN213760551U (en) | 1-butene refining energy-saving device with heat pump heat integration | |
| CN109701363A (en) | A method of methanol in recycling low temperature washing device for methanol sour gas | |
| CN203816465U (en) | Waste gas absorption tower | |
| CN203668270U (en) | Rectification device for vinyl toluene production | |
| CN102500193B (en) | Recovery and utilization method for tail gas in DMF (Dimethyfumarate) synthetic tower and device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |