CN105272807A - Multi-loop condensation technology for recovery of propylene in polypropylene device tail gas - Google Patents
Multi-loop condensation technology for recovery of propylene in polypropylene device tail gas Download PDFInfo
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- CN105272807A CN105272807A CN201510077819.2A CN201510077819A CN105272807A CN 105272807 A CN105272807 A CN 105272807A CN 201510077819 A CN201510077819 A CN 201510077819A CN 105272807 A CN105272807 A CN 105272807A
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Abstract
The invention discloses a multi-loop condensation technology for recovery of propylene in polypropylene device tail gas. For tail gas containing steam, firstly, drying processing is carried out or a frost prevention plug and a defrosting measure are arranged in the condensation process of the tail gas. A refrigerating unit is arranged, glycol refrigerated water is generated, and tail gas in different discharging points is condensed by glycol refrigerated water through heat exchangers respectively. Glycol refrigerated water and the tail gas in different discharging points are subjected to heat exchange in respective heat exchanges respectively, and the vast majority of propylene in the tail gas is condensed. Because ingredients and pressures of tail gas in different discharging points are different, respective condensation is selected, the self pressure of tail gas can be utilized, and propylene is recovered in an effective manner. In the obtained condensate liquid, the content of propylene is more than 90% (mass), the content of propylene and propane is more than 99.7% (mass), the total content of light components of hydrogen, nitrogen, C2 and the like is less than 0.15% (mass), and recovery of propylene is achieved indeed.
Description
Technical field
The invention belongs to technical field of petrochemical industry, specifically a kind of multiloop condensation process recycling propylene in polypropylene plant tail gas.
Background technology
Domestic polypropylene plant is divided into three kinds of techniques haply: liquid phase endless tube method, gas fluidized bed method, small scale bulk polymeric kettle method.These three kinds of techniques, in actual production, all can discharge a certain amount of tail gas, and its main component is propylene.For a set of 200,000 tons/year of liquid phase endless tube method polypropylene plants, its exhaust emissions has 3 points, sees the following form-1:
Table-1 liquid phase endless tube method polypropylene plant exhaust emissions point situation
Calculate by upper table-1, three strands of tail gas amount to 600kg/h, and wherein propylene is 531kg/h.If do not reclaimed tail gas, so this part tail gas enters full factory gas train and uses as fuel gas.
After adopting tail gas propylene recovery method of the present invention, propylene recovery rate gets 95% (wt), and polypropylene plant went into operation by 8000 hours the whole year, 1 year recyclable propylene 4036t.If fuel gas price is by 3000 yuan/t, propylene price is by 8000 yuan/t, and propylene recovery expense per ton 200 yuan/t, the propylene of recovery can increase value and be: ten thousand yuan, 4036 × (0.8-0.3-0.02)=1937.Therefore, exist and necessity of improving and improving carried out to existing polymarization method for prodcing polyacrylates flow process, come simple, reliable, safe, reclaim propylene in tail gas at low cost.
Domestic polypropylene plant, have the method such as membrane separation process, pressure swing adsorption process of employing Propylene recovery from tail gas, the problem that these method ubiquity recovering effects are bad, contrast the present invention, its investment is large, energy consumption is high, process is complicated.
According to statistics, China's polypropylene production in 2013 about 1,200 ten thousand tons, in the tail gas that these polypropylene plants discharge, potential propylene recovery amount is about 240,000 tons/year, and potential recovery value is about 1,200,000,000 yuan/year.Therefore, by the present invention, improve and improve the existing polypropylene plant technical process of China, a large amount of propylene can be reclaimed and bring huge economic benefit and social benefit.
Summary of the invention
The object of the present invention is to provide a kind of multiloop condensation process recycling propylene in polypropylene plant tail gas, with Propylene recovery in the tail gas discharged from polypropylene plant.
For achieving the above object, the invention provides following technical scheme:
A kind of multiloop condensation process recycling propylene in polypropylene plant tail gas, comprise three strands of tail gas, first strand of tail gas is the tail gas that decatize off-gas compressor is discharged, second strand of tail gas is the tail gas that CO stripper condenser is discharged, 3rd strand of tail gas is the tail gas that propylene condenser is discharged, first strand of tail gas contains moisture, and first strand of tail gas is one tail gas that pressure is minimum; The concrete steps of this technique are as follows:
A first () first strand of tail gas enter drying chamber (D-1AB) and remove moisture, then with ethylene glycol refrigerated water in the first tail gas condenser (E-1) heat exchange, condensation, then enter the first tail gas condensing tank (V-1);
B () second strand of tail gas and the heat exchange in the second tail gas condenser (E-2) of ethylene glycol refrigerated water, condensation, then enter the second tail gas condensing tank (V-2);
C () the 3rd strand of tail gas and the heat exchange in the 3rd tail gas condensing tank (E-3) of ethylene glycol refrigerated water, condensation, then enter the 3rd tail gas condensing tank (V-3);
(d) second tail gas condensing tank (V-2) non-condensable gas discharge, the first tail gas condensing tank (V-1) that phlegma goes pressure minimum;
(e) the 3rd tail gas condensing tank (V-3) non-condensable gas discharge, the first tail gas condensing tank (V-1) that phlegma goes pressure minimum;
F () first pressure of tail gas condensing tank (V-1) is minimum, it receives the tail gas of condensed first decatize off-gas compressor that the first tail gas condenser (E-1) comes and the phlegma that the second tail gas condensing tank (V-2), the 3rd tail gas condensing tank (V-3) come, equilibrium flash vaporization, non-condensable gas is discharged, and phlegma removes condensing propylene pump (P-1);
G phlegma is delivered to user by () condensing propylene pump (P-1);
H () unit cooler (PK-1) provides ethylene glycol refrigerated water by freezing water pot (V-4) and chilled water circulating pump (P-2) to the first tail gas condenser (E-1), the second tail gas condenser (E-2), the 3rd tail gas condensing tank (E-3).
As the further scheme of the present invention: described drying chamber (D-1AB) is arranged in parallel two.
As the further scheme of the present invention: the initial temperature of described ethylene glycol refrigerated water is between-19 DEG C-5 DEG C.
As the further scheme of the present invention: the non-condensable gas that in step (f), the first tail gas condensing tank (V-1), the second tail gas condensing tank (V-2), the 3rd tail gas condensing tank (V-3) are discharged, enters full factory gas train as fuel gas.
As the further scheme of the present invention: step (a) is replaced to: first first strand of tail gas enter the shell of the first tail gas condenser (E-1), ethylene glycol refrigerated water walks the tube side of the first tail gas condenser (E-1), then with the heat exchange in the first tail gas condenser (E-1) of ethylene glycol refrigerated water, condensation, the first tail gas condensing tank (V-1) is then entered.
Because first strand of tail gas contains moisture, so the heat-exchanging tube bundle outer wall of the first tail gas condenser (E-1) can hang frost and progressive additive, therefore, except taking suitable frost prevention bridging structure, also defrosting measure to be set.
As the further scheme of the present invention: described first tail gas condenser (E-1) selects DN600U shape tube heat-exchanger, and in the upper setting of described first tail gas condenser (E-1) at least two imports, to increase inlet area and number, and increase the external diameter of the first tail gas condenser (E-1), come frost-resistant stifled, be easy to ensure that condenser normally can use in 12 hours.
As the further scheme of the present invention: adopt defrosting measure as follows to the first tail gas condenser (E-1): using the first tail gas condenser (E-1) pressure difference signal or tail gas condensing temperature out or time setting as automatic defrosting program initiating signal; After defrosting program starts, its action precedence is: 1, open first burst of original voltage-controlled loop of tail gas, ensures that polypropylene plant is normally produced unaffected; 2, the import and export of the upper first strand of tail gas of the first tail gas condenser (E-1) are cut off; 3, the freezing water entrance of ethylene glycol of the first tail gas condenser (E-1) is cut off; 4, draw nitrogen at room and catch up with ethylene glycol refrigerated water in the tube side of clean first tail gas condenser (E-1); 5, draw nitrogen at room and replace first strand of tail gas in the shell of the first tail gas condenser (E-1), displacement gas enters fuel gas pipe network; 6, the shell that hot nitrogen purges dry first tail gas condenser (E-1) is drawn; 7, draw the shell of nitrogen at room cold blowing first tail gas condenser (E-1), defrosting completes; 8, open the freezing water entrance valve of ethylene glycol of the first tail gas condenser (E-1), ethylene glycol refrigerated water comes into operation; 9, open the first tail gas terminal valve of the first tail gas condenser (E-1), the first tail gas condenser (E-1) comes into operation; 10, first burst of original voltage-controlled loop of tail gas is closed; Whole defrosting program setting is 15-25 minute, within every 8-16 hour, runs once.
As the further scheme of the present invention: whole defrosting program setting is 20 minutes, within every 12 hours, run once.
The present invention, to the tail gas containing steam, first carries out drying treatment or in this burst of tail gas condensing process, arranges frost prevention blocking up and defrosting measure; Arrange unit cooler, produce ethylene glycol refrigerated water, spent glycol refrigerated water is by the tail gas of the different discharge point of interchanger difference condensation; The unit cooler adopted is common handpiece Water Chilling Units or other unit, and the ethylene glycol refrigerated water provided is refrigerated water or other medium; The tail gas heat exchange in respective interchanger respectively of ethylene glycol refrigerated water and different discharge point, the most propylene condensations in tail gas; Because its component of the tail gas of different discharge point is different with pressure, selects condensation respectively, the pressure itself of tail gas can be utilized, most effectively Propylene recovery.
The invention has the beneficial effects as follows:
The first, the initial temperature of ethylene glycol refrigerated water of the present invention is at-19 DEG C ~ 5 DEG C, and the material of such temperature range to equipment, pipeline etc. does not have particular requirement, and common unit cooler just can be held existing, and energy consumption is not high yet.
The second, the present invention utilizes the pressure of tail gas self, enables propylene condensation at a higher temperature, does not arrange tail-gas compressor, and process is simple effectively, energy consumption is low, it is low to invest.
Three, the pressure that the present invention is directed to different discharge point tail gas is different with composition, and adopt condensation respectively, can obtain best propylene recovery effect, the rate of recovery can reach 95% (quality).
4th, the phlegma that the tail gas of the different discharge point of the present invention produces through the freezing water cooling of ethylene glycol, enter the hydrops groove that respective condensate drum or interchanger carry respectively, finally converge to the minimum drainer of one of them pressure or hydrops groove, carry out equilibrium flash vaporization, the condensate converges obtained carries out equilibrium flash vaporization in the minimum condensate drum (or hydrops groove) of pressure, light constituent substantially flash distillation is gone out, in the phlegma obtained, propylene content is greater than 90% (quality), propylene plus propane content is greater than 99.7% (quality), hydrogen, nitrogen, the light constituent total contents such as C2 are less than 0.15% (quality), extract out after boosting through pump, can mix with the raw material propylene of polypropylene plant, also gas fractionation plant can be delivered to, really achieve the recovery of propylene.
Five, for the tail gas containing moisture, the present invention arranges drying facility or frost prevention blocks up condenser structure design and supporting automatic defrosting program, efficiently solves the frosting problem that tail gas aqueous brings.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention (when arranging drying facility).
Fig. 2 is process flow diagram of the present invention (when arranging the stifled and defrosting measure of frost prevention).
In figure: D-1AB is drying chamber, E-1 is PK-501 tail gas condenser, E-2 is E-701 tail gas condenser, E-3 is E-301 tail gas condenser, EH-1 is electric heater, V-1 is PK-501 tail gas condensing tank, V-2 is E-701 tail gas condensing tank, V-3 is E-301 tail gas condensing tank, V-4 is freezing water pot, P-1 is condensing propylene pump, P-2 is chilled water circulating pump, PK-1 is unit cooler.
Note: for ease of explanation, this process flow diagram device numbering relates to polypropylene plant, have references to the common numbering of domestic liquid phase endless tube method polypropylene plant, do not represent the recovery that present invention process is only applicable to liquid phase endless tube method polypropylene plant tail gas, but be applicable to comprise gas fluidized bed method allly have exhaust emissions and the polypropylene plant of propylene in tail gas need be reclaimed.
Embodiment
Be described in more detail below in conjunction with the technical scheme of embodiment to this patent.
Embodiment 1
The liquid phase endless tube method polypropylene plant of a set of annual output 200000 tons, the tail gas situation of its discharge sees above to be chatted " table 1 ".Condensation Propylene recovery process stream balance is in Table-2.
Table-2 material balance tables (8000h that goes into operation in year counts)
| Sequence number | Name of material | t/h | t/d | t/a | Remarks |
| Charging 1 | PK-501 (tail gas 1) | 0.4 | 9.6 | 3200 | Containing propylene 88.3% (quality) |
| Charging 2 | E-701 (tail gas 2) | 0.08 | 1.92 | 640 | Containing propylene 85.4% (quality) |
| Charging 3 | E-301 (tail gas 3) | 0.12 | 2.88 | 960 | Containing propylene 91.2% (quality) |
| Charging | Add up to | 0.6 | 14.4 | 4800 | |
| Discharging 1 | Phlegma | 0.556 | 13.344 | 4448 | Containing propylene 90.6% (quality) |
| Discharging 2 | Non-condensable gas | 0.044 | 1.056 | 352 | Containing propylene 61.7% (quality) |
| Discharging | Add up to | 0.6 | 14.4 | 4800 |
PK-501 tail gas (PK-501 gas steams the tail gas that off-gas compressor is discharged) temperature is 5 DEG C, pressure is 0.4MPa (gauge pressure, lower same), flow 400kg/h, containing saturation moisture [0.23% (mol), 0.0958% (wt)].
E-701 tail gas (tail gas that E-701CO stripper condenser is discharged) temperature is 50 DEG C, and pressure is 2.0MPa, flow 80kg/h.
E-301 tail gas (tail gas that E-301 propylene condenser is discharged) temperature is 25 DEG C, and pressure is 1.7MPa, flow 120t/h.
Refer to Fig. 1, a kind of multiloop condensation process recycling propylene in polypropylene plant tail gas, concrete steps are as follows:
(1) first the tail gas that PK-501 decatize off-gas compressor is discharged enter the drying chamber D-1AB that 3A molecular sieve desiccant is housed, and removes moisture to dew-point temperature lower than-20 DEG C.Drying chamber D-1AB comprises drying chamber D-1A and drying chamber D-1B, and drying chamber D-1A and drying chamber D-1B blocked operation, with nitrogen regeneration, every platform drying chamber is equipped with about 750kg molecular sieve, regeneration period is about 10 days, and regenerative process is about 16 hours, nitrogen use level be about 200 mark sides/hour; The tail gas of dried PK-501 decatize off-gas compressor, with the heat exchange of ethylene glycol refrigerated water in PK-501 tail gas condenser E-1, thermal load is 45kw, is cooled to-5 DEG C, is all condensed; Phlegma enters PK-501 tail gas condensing tank V-1, the phlegma mixed flash boiling come with E-701 tail gas condensing tank V-2, E-301 tail gas condensing tank V-3;
(2) E-701CO stripper condenser discharge tail gas in E-701 tail gas condenser E-2 with the heat exchange of ethylene glycol refrigerated water, thermal load is 8.3kw, be cooled to-5 DEG C, have the gas phase of 75% (mol) to be condensed, gas-liquid mixture enters E-701 tail gas condensing tank V-2; Non-condensable gas is discharged from E-701 tail gas condensing tank V-2 top, and flow is 16kg/h; Phlegma drains into PK-501 tail gas condensing tank V-1 from E-701 tail gas condensing tank V-2 bottom, and flow is 64kg/h;
(3) E-301 propylene condenser discharge tail gas in E-301 tail gas condensing tank E-3 with the heat exchange of ethylene glycol refrigerated water, thermal load is 13.6kw, be cooled to-5 DEG C, have the gas phase of 91% (mol) to be condensed, gas-liquid mixture enters E-301 tail gas condensing tank V-3; Non-condensable gas is discharged from E-301 tail gas condensing tank V-3 top, and flow is 7kg/h; Phlegma drains into PK-501 tail gas condensing tank V-1 from E-301 tail gas condensing tank V-3 bottom, and flow is 113kg/h;
(4) working pressure of PK-501 tail gas condensing tank V-1 is a little less than 0.4MPa; The working pressure of E-701 tail gas condensing tank V-2 is a little less than 2.0MPa; The working pressure of E-301 tail gas condensing tank V-3 is a little less than 1.7MPa; The phlegma that E-701 tail gas condensing tank V-2, E-301 tail gas condensing tank V-3 discharges enters PK-501 tail gas condensing tank V-1, because pressure reduces, flash distillation occurs, the light constituent overwhelming majority gasifications such as the hydrogen in phlegma, nitrogen; Because flash distillation, the temperature of PK-501 tail gas condensing tank V-1 is reduced to-10 DEG C, and the non-condensable gas flashed off is discharged from PK-501 tail gas condensing tank V-1 top, and flow is 21kg/h; Phlegma is extracted out from PK-501 tail gas condensing tank V-1 bottom by condensing propylene pump P-1, and flow is 556kg/h;
(5) non-condensable gas of PK-501 tail gas condensing tank V-1, E-701 tail gas condensing tank V-2, E-301 tail gas condensing tank V-3 discharge, enters full factory gas train as fuel gas;
(6) phlegma of PK-501 tail gas condensing tank V-1, after condensing propylene pump P-1 extracts out (shaft power of pump is 1.1kw), boosts to 2.2MPa, delivers to gas fractionation plant;
(7) unit cooler PK-1 provides ethylene glycol refrigerated water by freezing water pot V-4 and chilled water circulating pump P-2 to PK-501 tail gas condenser E-1, E-701 tail gas condenser E-2, E-301 tail gas condensing tank E-3; Described unit cooler PK-1 is refrigerating water sets, and the ethylene glycol refrigerated water provided is refrigerated water (mixture of water and antifreezing agent), and the leaving water temperature(LWT) of refrigerated water is-15 DEG C, and return water temperature is-5 DEG C, and refrigerating duty is 67kw, and current consumption is 22kw.
The energy consumption analysis of above-mentioned technological process is in Table-3.
Table-3 embodiment 1 energy consumption analysis
Note: adopt " petrochemical complex design energy consumption calculations method " SH/T3110-2001 to calculate.
Embodiment 2
The liquid phase endless tube method polypropylene plant of a set of annual output 200000 tons, the tail gas situation of its discharge sees above to be chatted " table-1 ".Condensation Propylene recovery process stream balance is in Table-4.
Table-4 material balance tables (8000h that goes into operation in year counts)
PK-501 tail gas (PK-501 gas steams the tail gas that off-gas compressor is discharged) temperature is 5 DEG C, pressure is 0.4MPa (gauge pressure, lower same), flow 400kg/h, containing saturation moisture [0.23% (mol), 0.0958% (wt), 0.38kg/h].
E-701 tail gas (tail gas that E-701CO stripper condenser is discharged) temperature is 50 DEG C, and pressure is 2.0MPa, flow 80kg/h.
E-301 tail gas (tail gas that E-301 propylene condenser is discharged) temperature is 25 DEG C, and pressure is 1.7MPa, flow 120t/h.
Refer to Fig. 2, a kind of multiloop condensation process recycling propylene in polypropylene plant tail gas, concrete steps are as follows:
(1) PK-501 gas steams the opening of tail gas by 2 DN200 of off-gas compressor discharge, enter the shell of E-301 tail gas condensing tank E-1, PK-501 tail gas condenser E-1 selects DN600U shape tube heat-exchanger, with the heat exchange of ethylene glycol refrigerated water in PK-501 tail gas condenser E-1, thermal load is 45kw, be cooled to-5 DEG C, be all condensed; Phlegma enters PK-501 tail gas condensing tank V-1, the phlegma mixed flash boiling come with E-701 tail gas condensing tank V-2, E-301 tail gas condensing tank V-3; Owing to containing moisture in tail gas, the heat-exchanging tube bundle outer wall of E-301 tail gas condensing tank E-1 can hang frost and progressive additive, and in 24 hours, semi-invariant is 9.197kg; Using condenser pressure difference signal or tail gas condensing temperature out or time setting as automatic defrosting program initiating signal.After defrosting program starts, its action precedence is: 1, open this burst of original voltage-controlled loop of tail gas, ensures that polypropylene plant is normally produced unaffected; 2, the import and export of condenser this strand of tail gas are cut off; 3, the freezing water entrance of condenser ethylene glycol is cut off; 4, draw nitrogen at room and catch up with ethylene glycol refrigerated water in clean condenser tube side; 5, draw the tail gas in nitrogen at room metathesis condensation device shell, displacement gas enters fuel gas pipe network; 6, draw hot nitrogen and purge dry condenser shell; 7, draw nitrogen at room cold blowing condenser shell, defrosting completes; 8, the freezing water entrance valve of open cold condenser ethylene glycol, ethylene glycol refrigerated water comes into operation; 9, open cold condenser tail gas terminal valve, condenser comes into operation; 10, this burst of original voltage-controlled loop of tail gas is closed.Whole defrosting program setting is 20 minutes, within every 12 hours, runs once.
(2) E-701CO stripper condenser discharge tail gas in E-701 tail gas condenser E-2 with the heat exchange of ethylene glycol refrigerated water, thermal load is 8.3kw, be cooled to-5 DEG C, have the gas phase of 75% (mol) to be condensed, gas-liquid mixture enters E-701 tail gas condensing tank V-2; Non-condensable gas is discharged from E-701 tail gas condensing tank V-2 top, and flow is 16kg/h; Phlegma drains into PK-501 tail gas condensing tank V-1 from E-701 tail gas condensing tank V-2 bottom, and flow is 64kg/h;
(3) E-301 propylene condenser discharge tail gas in E-701 tail gas condenser E-3 with the heat exchange of ethylene glycol refrigerated water, thermal load is 13.6kw, be cooled to-5 DEG C, have the gas phase of 91% (mol) to be condensed, gas-liquid mixture enters E-301 tail gas condensing tank V-3; Non-condensable gas is discharged from E-301 tail gas condensing tank V-3 top, and flow is 7kg/h; Phlegma drains into PK-501 tail gas condensing tank V-1 from E-301 tail gas condensing tank V-3 bottom, and flow is 113kg/h;
(4) working pressure of PK-501 tail gas condensing tank V-1 is a little less than 0.4MPa; The working pressure of E-701 tail gas condensing tank V-2 is a little less than 2.0MPa; The working pressure of E-301 tail gas condensing tank V-3 is a little less than 1.7MPa; The phlegma that E-701 tail gas condensing tank V-2, E-301 tail gas condensing tank V-3 discharges enters PK-501 tail gas condensing tank V-1, because pressure reduces, flash distillation occurs, the light constituent overwhelming majority gasifications such as the hydrogen in phlegma, nitrogen; Because flash distillation, the temperature of PK-501 tail gas condensing tank V-1 is reduced to-10 DEG C, and the non-condensable gas flashed off is discharged from PK-501 tail gas condensing tank V-1 top, and flow is 21kg/h; Phlegma is extracted out from PK-501 tail gas condensing tank V-1 bottom by condensing propylene pump P-1, and flow is 556kg/h;
(5) non-condensable gas of PK-501 tail gas condensing tank V-1, E-701 tail gas condensing tank V-2, E-301 tail gas condensing tank V-3 discharge, enters full factory gas train as fuel gas;
(6) phlegma of PK-501 tail gas condensing tank V-1, after condensing propylene pump P-1 extracts out (shaft power of pump is 1.1kw), boosts to 2.2MPa, delivers to gas fractionation plant;
(7) unit cooler PK-1 provides ethylene glycol refrigerated water by freezing water pot V-4 and chilled water circulating pump P-2 to PK-501 tail gas condenser E-1, E-701 tail gas condenser E-2, E-301 tail gas condensing tank E-3; Described unit cooler PK-1 is refrigerating water sets, and the ethylene glycol refrigerated water provided is refrigerated water (mixture of water and antifreezing agent), and the leaving water temperature(LWT) of refrigerated water is-15 DEG C, and return water temperature is-5 DEG C, and refrigerating duty is 67kw, and current consumption is 22kw.
The energy consumption analysis of above-mentioned technological process is in Table-5.
Table-5 embodiment 2 energy consumption analysis
Note: adopt " petrochemical complex design energy consumption calculations method " SH/T3110-2001 to calculate.
There is above-described embodiment 1 and 2 visible, the invention has the beneficial effects as follows:
The first, the initial temperature of ethylene glycol refrigerated water of the present invention is at-19 DEG C ~ 5 DEG C, and equipment, pipeline etc. do not need to select low temperature resistant material, and common unit cooler just can realize.
The second, the present invention utilizes the pressure of tail gas self, enables propylene condensation at a higher temperature, does not arrange tail-gas compressor, and process is simple effectively, energy consumption is low, it is low to invest.
Three, the pressure that the present invention is directed to different discharge point tail gas is different with composition, and adopt condensation respectively, can obtain best propylene recovery effect, the rate of recovery can reach 95% (quality).
Four, the condensate converges that obtains of the present invention carries out equilibrium flash vaporization in the minimum condensate drum (or hydrops groove) of pressure, light constituent substantially flash distillation is gone out, in the phlegma obtained, propylene content is greater than 90% (quality), propylene plus propane content is greater than 99.7% (quality), the light constituent total contents such as hydrogen, nitrogen, C2 are less than 0.15% (quality), really achieve the recovery of propylene.
Five, for the tail gas containing moisture, the present invention arranges drying facility or frost prevention blocks up condenser structure design and supporting automatic defrosting program, efficiently solves the frosting problem that tail gas aqueous brings.
Above the better embodiment of this patent is explained in detail, but this patent is not limited to above-mentioned embodiment, in the ken that one skilled in the relevant art possesses, can also makes a variety of changes under the prerequisite not departing from this patent aim.
Claims (8)
1. recycle the multiloop condensation process of propylene in polypropylene plant tail gas for one kind, described polypropylene plant tail gas comprises three strands of tail gas, first strand of tail gas is the tail gas that decatize off-gas compressor is discharged, second strand of tail gas is the tail gas that CO stripper condenser is discharged, 3rd strand of tail gas is the tail gas that propylene condenser is discharged, first strand of tail gas contains moisture, and first strand of tail gas is one tail gas that pressure is minimum; It is characterized in that, the concrete steps of this technique are as follows:
A first () first strand of tail gas enter drying chamber (D-1AB) and remove moisture, then with ethylene glycol refrigerated water in the first tail gas condenser (E-1) heat exchange, condensation, then enter the first tail gas condensing tank (V-1);
B () second strand of tail gas and the heat exchange in the second tail gas condenser (E-2) of ethylene glycol refrigerated water, condensation, then enter the second tail gas condensing tank (V-2);
C () the 3rd strand of tail gas and the heat exchange in the 3rd tail gas condensing tank (E-3) of ethylene glycol refrigerated water, condensation, then enter the 3rd tail gas condensing tank (V-3);
(d) second tail gas condensing tank (V-2) non-condensable gas discharge, the first tail gas condensing tank (V-1) that phlegma goes pressure minimum;
(e) the 3rd tail gas condensing tank (V-3) non-condensable gas discharge, the first tail gas condensing tank (V-1) that phlegma goes pressure minimum;
F () first pressure of tail gas condensing tank (V-1) is minimum, it receives the tail gas of condensed first decatize off-gas compressor that the first tail gas condenser (E-1) comes and the phlegma that the second tail gas condensing tank (V-2), the 3rd tail gas condensing tank (V-3) come, equilibrium flash vaporization, non-condensable gas is discharged, and phlegma removes condensing propylene pump (P-1);
G phlegma is delivered to user by () condensing propylene pump (P-1);
H () unit cooler (PK-1) provides ethylene glycol refrigerated water by freezing water pot (V-4) and chilled water circulating pump (P-2) to the first tail gas condenser (E-1), the second tail gas condenser (E-2), the 3rd tail gas condensing tank (E-3).
2. the multiloop condensation process of propylene in recycling polypropylene plant tail gas according to claim 1, it is characterized in that, described drying chamber (D-1AB) is arranged in parallel two.
3. the multiloop condensation process of propylene in recycling polypropylene plant tail gas according to claim 1, it is characterized in that, the initial temperature of described ethylene glycol refrigerated water is between-19 DEG C-5 DEG C.
4. the multiloop condensation process of propylene in recycling polypropylene plant tail gas according to claim 1, it is characterized in that, the non-condensable gas that in step (f), the first tail gas condensing tank (V-1), the second tail gas condensing tank (V-2), the 3rd tail gas condensing tank (V-3) are discharged, enters full factory gas train as fuel gas.
5. according to the multiloop condensation process of propylene in the recycling polypropylene plant tail gas one of claim 1-4 Suo Shu, it is characterized in that, step (a) is replaced to: first first strand of tail gas enter the shell of the first tail gas condenser (E-1), ethylene glycol refrigerated water walks the tube side of the first tail gas condenser (E-1), then with the heat exchange in the first tail gas condenser (E-1) of ethylene glycol refrigerated water, condensation, the first tail gas condensing tank (V-1) is then entered.
6. the multiloop condensation process of propylene in recycling polypropylene plant tail gas according to claim 5, it is characterized in that, described first tail gas condenser (E-1) selects DN600U shape tube heat-exchanger, and in the upper setting of described first tail gas condenser (E-1) at least two imports, and increase the external diameter of the first tail gas condenser (E-1).
7. the multiloop condensation process of propylene in recycling polypropylene plant tail gas according to claim 5, it is characterized in that, adopt defrosting measure as follows to the first tail gas condenser (E-1): using the first tail gas condenser (E-1) pressure difference signal or tail gas condensing temperature out or time setting as automatic defrosting program initiating signal; After defrosting program starts, its action precedence is: 1, open first burst of original voltage-controlled loop of tail gas, ensures that polypropylene plant is normally produced unaffected; 2, the import and export of the upper first strand of tail gas of the first tail gas condenser (E-1) are cut off; 3, the freezing water entrance of ethylene glycol of the first tail gas condenser (E-1) is cut off; 4, draw nitrogen at room and catch up with ethylene glycol refrigerated water in the tube side of clean first tail gas condenser (E-1); 5, draw nitrogen at room and replace first strand of tail gas in the shell of the first tail gas condenser (E-1), displacement gas enters fuel gas pipe network; 6, the shell that hot nitrogen purges dry first tail gas condenser (E-1) is drawn; 7, draw the shell of nitrogen at room cold blowing first tail gas condenser (E-1), defrosting completes; 8, open the freezing water entrance valve of ethylene glycol of the first tail gas condenser (E-1), ethylene glycol refrigerated water comes into operation; 9, open the first tail gas terminal valve of the first tail gas condenser (E-1), the first tail gas condenser (E-1) comes into operation; 10, first burst of original voltage-controlled loop of tail gas is closed; Whole defrosting program setting is 15-25 minute, within every 8-16 hour, runs once.
8. the multiloop condensation process of propylene in recycling polypropylene plant tail gas according to claim 7, it is characterized in that, whole defrosting program setting is 20 minutes, within every 12 hours, runs once.
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