CN104534709B - A kind of propylene flash distillation refrigeration process - Google Patents
A kind of propylene flash distillation refrigeration process Download PDFInfo
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- CN104534709B CN104534709B CN201410757912.3A CN201410757912A CN104534709B CN 104534709 B CN104534709 B CN 104534709B CN 201410757912 A CN201410757912 A CN 201410757912A CN 104534709 B CN104534709 B CN 104534709B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B1/00—Compression machines, plants or systems with non-reversible cycle
- F25B1/10—Compression machines, plants or systems with non-reversible cycle with multi-stage compression
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B31/00—Compressor arrangements
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
- F25B2400/00—General features or devices for refrigeration machines, plants or systems, combined heating and refrigeration systems or heat-pump systems, i.e. not limited to a particular subgroup of F25B
Abstract
The present invention relates to a kind of propylene flash distillation refrigeration process, it is characterised in that comprise the steps: that the gas-phase propene that user uses Posterior circle to return initially enters in one section of entrance knockout drum, after isolating liquid phase, enter propylene compressor from one-level entrance and be compressed；It is divided into five strands from propylene compressor gas-phase propene out, front four stocks do not send to four anti-surge pipelines, 5th strand deliver to cooler in be cooled to liquid propylene after carry out three stages of flashing successively, the gas-phase propene that flash distillation obtains respectively enters two to the level Four entrance of propylene compressor, sends to user and use after liquid propylene is supercool.The present invention can improve the efficiency of compressor, reduce the acting of compressor, reduce recirculated water usage amount, avoid flashed vapour simultaneously and be the most all decompressed to the high power consumption that low pressure is caused, improve liquid propylene and go out the degree of supercooling of battery limit (BL), reduce the propylene usage amount of refrigeration system, thus reduce the amount of one section of entrance gas-phase propene of compressor, reducing the power consumption of compressor, energy conservation and consumption reduction effects is notable.
Description
Technical field
The present invention relates to a kind of propylene flash distillation refrigeration process.
Background technology
Refrigeration modes mainly has three kinds, compression refrigeration and absorption refrigeration and compression and absorption hybrid refrigeration.Industrial often
That sees has propylene compression refrigeration, ammonia compression refrigeration etc..Civilian cold-producing medium can use Freon 12 and chlorodifluoromethane as system
Cryogen, for central air-conditioning, air conditioning for automobiles, refrigerator ice cabinet, freezer etc..
In large-scale coal chemical engineering equipment now, low-temp methanol washing process is the most all used to carry out the purification of gas with desulfurization
Decarburization, and the refrigeration requirement of unit is washed in order to meet low-temp methanol, need configuration ice maker unit to provide cold, ice maker unit can
The cold-producing medium used has propylene and ammonia etc..The most especially the propylene compression refrigerating system with propylene as cold-producing medium and low-temp methanol is washed
Combination configuration is most commonly seen.
The flow process of propylene compression refrigeration is relatively simple, carrys out configuration flow mainly around propylene compressor.Low-temp methanol washes unit
The cold needed generally-40 DEG C, the aftercooler of compressor bank typically uses circulating water, the liquid of water recirculator outlet
Phase propylene is typically by 43 DEG C of considerations, and when 43 DEG C, the saturated vapor pressure of propylene is 1.69MPaG, it is considered to the pressure drop of water recirculator,
Then the outlet compression of propylene compressor designs generally according to 1.78MPaG, washes unit through low-temp methanol and absorbs cold, after using
Propylene be-40 DEG C, the saturated vapor pressure of propylene is 0.039MPaG, i.e. one section of inlet pressure of compressor is 0.039MPaG, temperature
Degree is for-40 DEG C.
In general, above-mentioned setting is all identical in each commercial plant.Difference is, the QI invigorating that compressor uses
Hop count, and the cryogenic energy utilization of the energy-conservation refrigeration of propylene.The flow setting of conventional propylene refrigeration system is as follows: through propylene compressor
Gas-phase propene after compression, enters water recirculator cooling, after being cooled to the liquid propylene of 43 DEG C, enters propylene collecting tank,
The liquid propylene gone out bottom propylene collecting tank, is divided into two strands, and one removes the tube side of propylene subcooler, and one goes propylene supercool
The shell side of device, walks that strand of liquid propylene of propylene subcooler shell side, and first passing through air relief valve JL-1 vacuum flashing is 0.55MPaG,
The gas-liquid two-phase of 3.4 DEG C, the propylene for tube side cools down offer cold, by the propylene supercooling of tube side to 10 DEG C, delivers to out-of-bounds
Low-temp methanol washes unit, the cold needed for providing for it.That strand of propylene of shell side, gas phase goes the separation of compressor two-stage nitration entrance
Tank, after isolating liquid phase, the two-stage nitration QI invigorating as compressor enters propylene compressor.
Summary of the invention
The technical problem to be solved is that the present situation for prior art provides a kind of three grades of propylene flash distillations refrigeration
Technique, thus reach to save equipment investment, energy consumption is greatly lowered, thus reduce the operating cost of refrigeration system.
The present invention solves the technical scheme that above-mentioned technical problem used: this propylene flash distillation refrigeration process, its feature exists
In comprising the steps:
The gas-phase propene that user uses Posterior circle to return initially enters in one section of entrance knockout drum, after isolating liquid phase, from
One-level entrance enters propylene compressor and is compressed；
Propylene from two-stage nitration entrance knockout drum enters propylene compressor from secondary inlet；
Propylene from three sections of entrance knockout drums enters propylene compressor from three grades of entrances；
Propylene from four sections of entrance knockout drums enters propylene compressor from level Four entrance；
Wherein said one-level entrance is the Initial Entry of propylene compressor, is arranged on the original position of propylene compressor；Institute
State secondary inlet and be arranged on the position that propylene compressor pressure is 0.1-0.55MPaG；Described three grades of entrances are arranged on propylene compression
Machine pressure is the position of 0.29-1.0MPaG；Described level Four entrance is arranged on the position that propylene compressor pressure is 0.55-1.5MPaG
Put；And the pressure of next stage entrance is more than the pressure of adjacent upper level entrance；
It is divided into five strands from propylene compressor gas-phase propene out, wherein delivers to one by the first anti-surge pipeline for first strand
Section entrance knockout drum；Two-stage nitration entrance knockout drum is delivered to for second strand by the second anti-surge pipeline；3rd strand is passed through the 3rd anti-surge
Three sections of entrance knockout drums delivered to by pipeline；Four sections of entrance knockout drums are delivered to for 4th strand by the 4th anti-surge pipeline；Enter each anti-asthma
The amount of the gas-phase propene shaken in line, to ensure that the air inflow of each section of entrance of compressor is not less than the pumping point of compressor and is as the criterion.When
When the air inflow of each section of suction port of compressor is less than compressor surge point, corresponding anti-surge valve is opened, and is mended by each anti-surge line
It is charged into tolerance, makes each section of inlet induction amount of compressor be at least up to the pumping point requirement of compressor, to prevent breathing heavily of compressor
Shake the damage to body.
5th strand deliver to cooler in be cooled to liquid propylene after after being decompressed to 0.55-1.5MPaG by the first air relief valve
Enter described four sections of entrance knockout drums；In four sections of entrance knockout drums, isolated gas phase is from the gaseous phase outlet of four sections of entrance knockout drums
Return described level Four entrance, four sections of isolated liquid phases of entrance knockout drum from the liquid-phase outlet of four sections of entrance knockout drums via second
Air relief valve enters in three sections of entrance knockout drums after being decompressed to 0.29-1.0MPaG；
It is back to described three grades from the gaseous phase outlet of three sections of entrance knockout drums through three sections of isolated gas phases of entrance knockout drum
Entrance, three sections of isolated liquid phases of entrance knockout drum are divided into two strands after going out three sections of entrance knockout drums, and wherein the first stock-traders' know-how is by
Three air relief valve enter in subcooler as refrigerant after being decompressed to 0.1-0.55MPaG, with the second burst of liquid phase entering subcooler
Propylene heat exchange, second burst of liquid propylene heat exchange is sent to user to-26～8 DEG C and is used, return described one section of entrance after heat exchange
Knockout drum；In first strand of entrance two-stage nitration entrance knockout drum after heat exchange, after isolating liquid phase, send into described secondary inlet.
Preferably, pressure more than the height 0.061MPa of one-level entrance described in the pressure ratio of described secondary inlet, described three grades
Pressure more than the height 0.19MPa of secondary inlet described in the pressure ratio of entrance, three grades of entrances described in the pressure ratio of described level Four entrance
Pressure more than height 0.26MPa.
Described propylene compressor is preferably steam drive turbocompressor.
The present invention is provided with three QI invigorating imports at the different pressure position of propylene compressor, uses three stages of flashing three sections
QI invigorating, fills into the gas-phase propene of different pressures respectively at three QI invigorating entrances, to improve the efficiency of compressor, reduces compressor
Acting, can raise the temperature that compression process produces simultaneously and alleviate, save the consumption of the merit that volumetric expansion brings, improve
The efficiency of compressor, the most also can reduce the outlet temperature of compressor, reduces cooling water water usage amount；Utilize three stages of flashing by liquid
Phase propylene is lowered the temperature step by step, split reduction, it is to avoid flashed vapour is disposably decompressed to high power problems that low pressure is caused, saves pressure
Contracting merit, and improve liquid propylene and go out the degree of supercooling of battery limit (BL), decrease the propylene usage amount of refrigeration system, thus reduce compression
The amount of one section of entrance gas-phase propene of machine, reduces the power consumption of compressor, and energy conservation and consumption reduction effects is notable.
By above-mentioned measure, the circulating load of liquid phase low temperature propylene can be made to reduce, the propylene degree of supercooling going out battery limit (BL) is lower, thus
The utilization rate making propylene improves, and whole refrigeration system is more energy-conservation；Propylene self-cooled heat exchanger i.e. propylene subcooler size simultaneously
Reducing therewith, the consumption of propylene self-cooled heat exchanger shell pass propylene reduces the most therewith, reduce further the power consumption of compressor；And
And the flash distillation cooling of propylene and separation combine, complete within one device, save equipment investment.
Compared with prior art, the present invention saves work done during compression 16%～8% according to circulating water entirety, if selecting
Chilled water cooling at most can save work done during compression 42.8%.
Accompanying drawing explanation
Fig. 1 is embodiment of the present invention flow chart.
Detailed description of the invention
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
Embodiment 1 to embodiment 5
To support the use, this propylene flash distillation refrigeration process is described in low-temp methanol is washed.
As it is shown in figure 1, the technological process of each embodiment is as follows:
Initially enter in one section of entrance knockout drum 1 with the most 1. logistics of the gas-phase propene after heat exchange of methanol, after isolating liquid phase,
Obtaining 2. number logistics, 2. number logistics enters propylene compressor 3 from one-level entrance a, is compressed propylene compressor 3 one sections；One
Level entrance a is the Initial Entry of propylene compressor 3, is arranged on the original position of propylene compressor.
Gas-phase propene from two-stage nitration entrance knockout drum 7 enters propylene compressor 3 from secondary inlet b, and through one section of compression
Gas-phase propene mixing after enter propylene compressor two-stage nitration together and be compressed, secondary inlet b arranges propylene compressor pressure and is
0.1-0.55MPaG position；
Gas-phase propene from three sections of entrance knockout drums 8 enters propylene compressors 3 from three grades of entrance c, and through compressor two
Enter propylene compressor three sections together after the gas-phase propene mixing of section compression to be compressed；Three grades of entrances are arranged on propylene compressor
Pressure is the position of 0.29-1.0MPaG；
From four sections of entrance knockout drums 5 gas-phase propene from level Four entrance d return propylene compressor, with through three sections compression
Enter propylene compressor four sections together after gas-phase propene mixing to be compressed,；Level Four entrance d is arranged on propylene compressor pressure
The position of 0.55-1.5MPaG.
The 3. logistics going out propylene compressor is divided into five strands, respectively one section anti-surge line 31, two-stage nitration anti-surge line 32, three sections
33, four sections of anti-surge lines 34 of anti-surge line and propylene compressor Trunk Line 13.
It is divided into five strands from propylene compressor gas-phase propene out, is wherein delivered to by the first anti-surge pipeline 31 for first strand
One section of entrance knockout drum 1；Two-stage nitration entrance knockout drum 7 is delivered to for second strand by the second anti-surge pipeline 32；3rd strand is passed through the 3rd
Three sections of entrance knockout drums 8 delivered to by anti-surge pipeline 33；Four sections of entrance knockout drums are delivered to for 4th strand by the 4th anti-surge pipeline 34
5。
When oepration at full load, the valve closing on each section of anti-surge line of compressor, at compressor each section of entrance a, b, c, d
Air inflow less than pumping point time, the valve on corresponding anti-surge line automatically opens up, to corresponding suction port of compressor QI invigorating.Enter each
The amount of the gas-phase propene in anti-surge line is not less than the surge of compressor with each section of entrance a, b, c, d air inflow ensureing compressor
Point, thus avoid the surge of compressor.
During underload, the gas-phase propene from one section of anti-surge line removes one section of entrance knockout drum 1 of compressor after decompression, subtracts
Gas-phase propene after pressure in one section of entrance knockout drum 1 with the liquid propylene heat exchange of-40 DEG C, liquid propylene is evaporated into-40 DEG C
Gas-phase propene, subsequently into one section of entrance of compressor, the liquid propylene evaporated can be by the part third from propylene subcooler 6
Alkene supplements.Equally, the gas-phase propene from two-stage nitration anti-surge line removes compressor two-stage nitration entrance knockout drum 7, after decompression after decompression
Gas-phase propene in compressor two-stage nitration entrance knockout drum 7 with from propylene subcooler 6 liquid propylene heat exchange, liquid propylene
Being evaporated to gas-phase propene, subsequently into compressor two-stage nitration entrance, the liquid propylene evaporated is by the portion from propylene subcooler 6
Propylene is divided to supplement.
Similarly, the gas-phase propene from three sections of anti-surge lines removes three sections of entrance knockout drums 8 of compressor after decompression, decompression
After gas-phase propene in three sections of entrance knockout drums 8 of compressor with from four sections of entrance knockout drums 5 of compressor through decompression gas-liquid
Biphase propylene heat exchange, liquid propylene is evaporated to gas-phase propene, subsequently into three sections of entrances of compressor.
Gas-phase propene from four sections of anti-surge lines removes four sections of entrance knockout drums 5 of compressor after decompression, and carrys out self-loopa
The gas-liquid two-phase propylene heat exchange through decompression of water cooler 4, liquid propylene is evaporated to gas-phase propene, subsequently into compressor four
Section entrance.
Finally one is that the 5th strand of cooled device 4 is cooled to liquid propylene, and i.e. logistics is 4., through the first air relief valve decompression is
The gas-liquid two-phase propylene of 0.55-1.5MPaG, enters four sections of entrance knockout drums 5；Isolated gas phase in four sections of entrance knockout drums 5
Propylene the most 5. logistics returns level Four entrance d from the gaseous phase outlet of four sections of entrance knockout drums, as four sections of QI invigorating of propylene compressor；
Isolated liquid phase enters three sections of entrances separation after the second air relief valve decompression is for gas-liquid two-phase that pressure is 0.29-1.0MPaG
Tank 8.
Propylene compressor is returned from three grades of entrance c via three sections of entrance knockout drum 8 isolated gas-phase propene the most 6. logistics,
Isolated liquid phase is divided into two strands after going out three sections of entrance knockout drums 8, second strand of tube side walking propylene subcooler, walks propylene for first strand
The shell side of subcooler.Wherein first strand of propylene enters third as cooling medium after the 3rd air relief valve is decompressed to 0.1-0.55MPaG
The shell side of alkene subcooler 6, with second burst of propylene heat exchange in tube side, provides cold for second strand of liquid propylene.Shell side afterwards
Gas-phase propene is sent to two-stage nitration knockout drum, isolate gas-phase propene the most 7. logistics from secondary inlet b return propylene compressor, second strand
It is too cold the 8. logistics obtained and delivers to user's use, with heat exchange of methanol.
In embodiment 1 to embodiment 5, each flow stream parameters is as shown in table 1.
Table 1
| 1. logistics | 2. logistics | 3. logistics | 4. logistics | 5. logistics | 6. logistics | 7. logistics | 8. logistics | ||
| Embodiment 1 | Temperature/DEG C | -40 | -40 | 80 | 44.5 | 22.6 | 3.4 | -31 | -26 |
| Pressure/MPaG | 0.039 | 0.039 | 1.78 | 1.755 | 1.0 | 0.55 | 0.1 | 0.5 | |
| Embodiment 2 | Temperature/DEG C | -40 | -40 | 75 | 39.5 | 22.6 | 3.4 | -31 | -26 |
| Pressure/MPaG | 0.039 | 0.039 | 1.58 | 1.555 | 1.0 | 0.55 | 0.1 | 0.5 | |
| Embodiment 3 | Temperature/DEG C | -40 | -40 | 44 | 12 | 3.4 | -13 | -31 | -26 |
| Pressure/MPaG | 0.039 | 0.039 | 0.75 | 0.725 | 0.55 | 0.29 | 0.1 | 0.5 | |
| Embodiment 4 | Temperature/DEG C | -40 | -40 | 78.8 | 42 | 38 | 22.6 | 3.4 | 8.4 |
| Pressure/MPaG | 0.039 | 0.039 | 1.68 | 1.655 | 1.5 | 1.0 | 0.55 | 0.95 | |
| Embodiment 5 | Temperature/DEG C | -40 | -40 | 75 | 39.5 | 19.7 | 1.8 | -21 | -16 |
| Pressure/MPaG | 0.039 | 0.039 | 1.58 | 1.555 | 0.92 | 0.52 | 0.2 | 0.47 |
The electricity charge are calculated by 0.58 yuan/degree, and the time of running in device year is 8000 hours, the operation energy of embodiment 1 to embodiment 5
Consumption is as shown in table 2.
Table 2
| Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 | Comparative example | |
| Power/KW | 7334 | 6810 | 4194 | 7371 | 6743 | 8018 |
| Operating cost (ten thousand yuan/year) | 3402.976 | 3159.84 | 1946.016 | 3420.144 | 3128.752 | 3720.352 |
| Save (ten thousand yuan/year) | 317.376 | 560.512 | 1774.336 | 300.208 | 591.6 |
In upper table, listed comparative example refers to the conventional propylene cooling flow under same size.In the various embodiments described above, pass through
By the liquid propylene after circulating water, carry out classification flash distillation, lower the temperature step by step, the gas-phase propene that classification flashes off, fill into respectively
Compressor entrance at different levels, reduces the outlet pressure of compressor, thus has reached to save the acting effect of compressor.
Embodiment 1,2 and embodiment 4,5 use conventional circulating water, and compressor delivery pressure is minimum is down to
1.58MPaG, arranges compared with the outlet pressure of 1.78MPaG with old process, can save the power consumption about 7.5% of compressor.
Embodiment 3 uses chilled water to carry out heat exchange, and by the upper coolant-temperature gage 7 DEG C of chilled water, return water temperature 12 DEG C, under being condensed by it
The temperature of the liquid propylene come is 12 DEG C, and when 12 DEG C, the pressure of propylene is 0.725MPaG, then the outlet pressure of compressor can control
To 0.75MPaG, the compressor delivery pressure of relative 1.78MPaG can save the power consumption about 42.8% of compressor.
Liquid propylene after cooling separates through three stages of flashing, respectively using three stages of flashing gas phase as the three of propylene compressor
Section QI invigorating, can reduce the temperature of compressor gas to reduce the volume of gas, thus save the work done during compression of compressor, reduces system
The turbine of system drives steam consumption quantity.
The heat transfer process of propylene is optimized, by the cooling in the first order of propylene and second level flash distillation and separation process
Combine, complete the most within one device, save equipment investment.
By the three stages of flashing of liquid propylene, propylene is divided into three grades of coolings, it is to avoid flashed vapour is the most all decompressed to
Low pressure, saves work done during compression about 8.5%, can suitably reduce again the load of propylene subcooler, reduces the size of this heat exchanger, reduces system
Investment cost of cooling system.
The temperature that liquid propylene goes out battery limit (BL) is lower, improves the utilization rate of propylene, reduces the circulating load of liquid propylene, saves
The operating cost of refrigeration system about 4%, so that whole refrigeration system is more energy-conservation.
Claims (3)
1. a propylene flash distillation refrigeration process, it is characterised in that comprise the steps:
The gas-phase propene that user uses Posterior circle to return initially enters in one section of entrance knockout drum (1), after isolating liquid phase, from one
Level entrance (a) enters propylene compressor (3) and is compressed；
Propylene from two-stage nitration entrance knockout drum (7) enters propylene compressor (3) from secondary inlet (b)；
Propylene from three sections of entrance knockout drums (8) enters propylene compressor (3) from three grades of entrances (c)；
Propylene from four sections of entrance knockout drums (5) enters propylene compressor (3) from level Four entrance (d)；
Wherein said one-level entrance (a) is the Initial Entry of propylene compressor (3), is arranged on the original position of propylene compressor；
It is 0.1-0.55MPaG position that described secondary inlet (b) arranges propylene compressor pressure；Described three grades of entrances (c) are arranged on propylene
Compressor pressure is the position of 0.29-1.0MPaG；It is 0.55-that described level Four entrance (d) is arranged on propylene compressor pressure
The position of 1.5MPaG；And the pressure of next stage entrance is more than the pressure of adjacent upper level entrance；
It is divided into five strands from propylene compressor gas-phase propene out, wherein delivers to one by the first anti-surge pipeline (31) for first strand
Section entrance knockout drum (1)；Two-stage nitration entrance knockout drum (7) is delivered to for second strand by the second anti-surge pipeline (32)；3rd strand is passed through
Three sections of entrance knockout drums (8) delivered to by 3rd anti-surge pipeline (33)；Four sections are delivered to for 4th strand by the 4th anti-surge pipeline (34)
Entrance knockout drum (5)；Enter the amount of the gas-phase propene in each anti-surge line should ensure that compressor each section of entrance air inflow not
Pumping point less than compressor；
5th strand deliver to cooler (4) in be cooled to liquid propylene after through being decompressed to 0.55-1.5MPaG by the first air relief valve (16)
The described four sections of entrance knockout drums (5) of rear entrance；In four sections of entrance knockout drums (5), isolated gas phase is from four sections of entrance knockout drums
Gaseous phase outlet returns described level Four entrance (d), and four sections of isolated liquid phases of entrance knockout drum (5) are from the liquid of four sections of entrance knockout drums
Export mutually and enter in three sections of entrance knockout drums (8) after being decompressed to 0.29-1.0MPaG via the second air relief valve (15)；
Described three grades of entrances are returned from the gaseous phase outlet of three sections of entrance knockout drums through three sections of isolated gas phases of entrance knockout drum (8)
(c), three sections of isolated liquid phases of entrance knockout drum (8) are divided into two strands after going out three sections of entrance knockout drums, wherein the first stock-traders' know-how by
3rd air relief valve (14) enters in subcooler (6) as refrigerant after being decompressed to 0.1-0.55MPaG, with entrance subcooler
Second burst of liquid propylene heat exchange, second burst of liquid propylene heat exchange is sent to user to-26～8 DEG C and is used, return institute after heat exchange
State one section of entrance knockout drum (1)；In first burst of entrance two-stage nitration entrance knockout drum (7) after heat exchange, after isolating liquid phase, send into institute
State secondary inlet (b).
Propylene flash distillation refrigeration process the most according to claim 1, it is characterised in that the pressure ratio institute of described secondary inlet (b)
State pressure more than the height 0.061MPa of one-level entrance (a), the pressure of secondary inlet (b) described in the pressure ratio of described three grades of entrances (c)
Power more than height 0.19MPa, pressure more than the height 0.26MPa of three grades of entrances (c) described in the pressure ratio of described level Four entrance (d).
Propylene flash distillation refrigeration process the most according to claim 1, it is characterised in that described propylene compressor is steam drive
Turbocompressor.
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