WO2015033935A1 - Procédé et usine pour l'utilisation de vapeur recomprimée - Google Patents

Procédé et usine pour l'utilisation de vapeur recomprimée Download PDF

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WO2015033935A1
WO2015033935A1 PCT/JP2014/073086 JP2014073086W WO2015033935A1 WO 2015033935 A1 WO2015033935 A1 WO 2015033935A1 JP 2014073086 W JP2014073086 W JP 2014073086W WO 2015033935 A1 WO2015033935 A1 WO 2015033935A1
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steam
gas
unit
line
main
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PCT/JP2014/073086
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English (en)
Japanese (ja)
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充宏 河野
木村　聡
亀井　登
和久 当房
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株式会社ダイセル
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Priority to CN201480049180.0A priority Critical patent/CN105517682B/zh
Priority to JP2015535484A priority patent/JP6291499B2/ja
Publication of WO2015033935A1 publication Critical patent/WO2015033935A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0033—Other features
    • B01D5/0039—Recuperation of heat, e.g. use of heat pump(s), compression
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression

Definitions

  • the present invention relates to a utilization method of recompressed steam in which the steam is adiabatically compressed by a compressor and efficiently reused as a heat source in a process involving generation of steam, and a plant using the method.
  • Vapor recompression is a technology that adiabatically compresses and raises the temperature by using a compressor in a vapor phase process containing steam.
  • the use of compressed steam whose temperature has been increased by this technique has been studied to use its latent heat or sensible heat as a heat source for processes such as evaporation, distillation, and drying.
  • VRC process VRC process
  • the compressor that is the core equipment of the VRC process has restrictions that should be observed from the viewpoint of equipment protection in operation, and this restriction makes it difficult to apply VRC.
  • an upper limit is usually set for the application temperature regardless of the type.
  • the clearance between the female and male rotors is reduced with thermal expansion, so that an upper limit value is set for the gas suction temperature in order to prevent contact and breakage. Therefore, when the gas suction temperature exceeds the upper limit value, the operation must be stopped to protect the equipment.
  • a cooler is required, which increases equipment costs.
  • the turbo type there is a case where the process gas stays without condensing due to a heat transfer failure or the like in an air supply destination device using compressed gas as a heat source.
  • the intake gas to the compressor is extremely reduced due to various causes such as the inability to continuously supply air from the compressor. This is likely to cause equipment damage. Problems that lead to damage to these devices are particularly likely to occur when switching the heat source to the VRC process, and it is necessary to take some measures for ensuring safety, but no effective measures have been proposed yet. .
  • Patent Document 1 in a solvent recovery method using a heat pump method (vapor recompression method) from a stock solution containing non-volatile substances, steam is supplied from the top line of the heat pump distillation column to the vapor compressor.
  • a method is disclosed in which after introducing, increasing the pressure and raising the temperature, a reboiler provides the necessary amount of heat to the distillation column.
  • an object of the present invention is to provide a method for reusing process steam whose temperature has been increased by adiabatic compression safely and simply as a heat source and a plant using this method.
  • the present inventors have provided a heat exchange step in a method in which recompressed steam obtained by adiabatically compressing process steam (vapor recompression; VRC) is used as a heat source.
  • VRC vapor recompression
  • the method of using recompressed steam of the present invention comprises a main process for generating process steam, which is a condensable gas, and recovering the generated process steam as a condensate, and at least part of the process steam by a compressor.
  • process steam which is a condensable gas
  • recovering the generated process steam as a condensate, and at least part of the process steam by a compressor Among the recompressed steam that was subjected to adiabatic compression and increased in temperature to obtain recompressed steam, the heat exchange process that uses the recompressed steam as a heat source, and the recompressed steam used in the heat exchange process, it did not condense A circulation step for returning the gas component to the main step.
  • the main process for example, a part of the generated process steam is cooled and condensed, and in the steam recompression process, the remainder of the process steam is adiabatically compressed by a compressor to increase the temperature and recompressed steam.
  • You may get In the main step after the process fluid obtained by condensing the process vapor and the gas component from the circulation step are merged, the merged mixture may be cooled and condensed.
  • the method of the present invention further includes a gas-liquid separation step for gas-liquid separation of the process fluid that has undergone the heat exchange step, and the gas component separated in the gas-liquid separation step may be returned to the main step in the circulation step. Good.
  • the compression ratio in the vapor recompression step may be controlled by adjusting the flow rate of the gas component that is returned (circulated) to the main step.
  • the main process may include a distillation process.
  • recompressed steam may be used as a heat source for the main step.
  • a steam generator for generating process steam which is a condensable gas
  • a main unit having a condenser for cooling and condensing a part of the generated process steam, and the rest of the process steam is adiabatically compressed.
  • the steam recompression unit for increasing the temperature to obtain recompressed steam, the heat exchange unit for using the recompressed steam as a heat source, and the recompressed steam provided to the heat exchange unit are condensed.
  • a recompressed steam utilization plant with a circulation line for returning the missing gas components to the main unit.
  • the main unit includes a discharge line for discharging process steam and a condenser (single condenser) connected to the discharge line, and the discharge line supplies a part of the process steam to the condenser.
  • a circulation line may be connected to a line upstream of the condenser of the main unit.
  • the main unit includes a discharge line for discharging the process steam and a plurality of condensers connected in series and sequentially arranged.
  • the discharge line supplies a part of the process steam to the first condenser.
  • the circulation line is downstream from the first condenser of the main unit and upstream from the last condenser. May be connected to the other line.
  • the plant of the present invention may further include a gas-liquid separation unit for gas-liquid separation of the process fluid that has passed through the heat exchange unit and returning the separated gas components to the main unit.
  • the circulation line may be provided with a flow rate control unit capable of adjusting the compression ratio in the vapor recompression unit by adjusting the flow rate of the gas component returning (circulated) to the main unit.
  • the main unit may include a distillation column. In the heat exchange unit, recompressed steam may be used as a heat source for the main unit.
  • process steam means steam generated in a manufacturing process (step) in which a unit operation involving a gas-liquid phase change is incorporated
  • compressed steam means steam recycle.
  • VRC compression system
  • the gas component that has not been condensed is returned to the main process (main process).
  • main process main process
  • resource-saving energy-saving equipment can use recompressed steam as a heat source, and can provide a utilization method and plant with excellent design and operation flexibility and controllability.
  • FIG. 1 is a process flow diagram for explaining an example of a utilization method and plant (apparatus) of recompressed steam according to the present invention.
  • FIG. 2 is a process flow diagram for explaining the method and apparatus for using recompressed steam according to the first embodiment.
  • FIG. 3 is a process flow diagram for explaining a method and apparatus for using recompressed steam according to Comparative Example 1.
  • FIG. 4 is a process flow diagram for explaining a method and apparatus for using recompressed steam according to the second embodiment.
  • FIG. 5 is a process flow diagram for explaining a method and apparatus for using recompressed steam according to Comparative Example 3.
  • the recompressed steam utilization plant includes a distillation tower 1 as a process steam generator that discharges process steam that is a condensable gas, and the process steam is discharged from the distillation tower 1.
  • the discharge line branches at a branch point 4.
  • One of the branched lines is provided with a first condenser 2 and a second condenser 3 for cooling and condensing a part of the process steam discharged from the distillation column 1, and the process steam is cooled by the condenser. And recovered as a condensate.
  • the main unit includes the distillation column 1, the first condenser 2 and the second condenser 3.
  • the remaining portion of the process steam is adiabatically compressed through a line in which a flow rate control valve (valve) 15 as a flow rate control unit is disposed, and the temperature is increased to recompress the steam.
  • a screw-type compressor 5 as a steam recompression unit for obtaining the heat
  • a heat exchanger 7 as a heat exchange unit for using the recompressed steam as a heat source
  • a process fluid that has passed through the heat exchanger 7 is gas-liquid separated.
  • a gas-liquid separator 8 as a gas-liquid separation unit for returning the separated gas component to the main unit is provided.
  • the process fluid that has passed through the heat exchanger 7 is further separated into a gas component and a liquid component (condensate), and the separated condensate is a flow rate control valve 13 as a flow rate control unit.
  • the gas component separated by the gas-liquid separator 8 is returned to the main unit by the first circulation line 9 together with the gas from the air ring line of the heat exchanger 7.
  • the first circulation line 9 is connected to a line between the first capacitor 2 and the second capacitor 3 via a connection portion 10, and is joined with the process fluid that has passed through the first capacitor 2. Then, it is cooled and condensed by the second condenser and recovered.
  • the screw type compressor 5 is provided with a second circulation line 6 for connecting the inlet side line and the outlet side line of the compressor, and a flow rate control valve 12 as a flow rate control unit. Also good.
  • the utilization method or plant of this invention contains the distillation column 1, the 1st condenser 2, and the 2nd condenser 3 as needed, generates the process vapor
  • a VRC process VRC process
  • the operation is performed only in the main process before the start of the VRC process. That is, the flow rate control valve 15 is closed, and the process steam discharged from the distillation column 1 is cooled and condensed by the first condenser 2 and the second condenser 3 and recovered as a condensate. Next, the flow rate control valves 11, 12, and 15 are fully opened, the screw type compressor 5 is started with the flow rate control valve 13 closed, and is stabilized at the rated rotational speed. At this time, a part of the process steam discharged from the distillation column 1 is sucked to the compressor 5 side through the branch point 4 of the discharge line of the main process, and is replaced with the seal gas of the line in the VRC process.
  • the process steam passing through the screw compressor 5 is hardly loaded with a discharge pressure, but the process is such that the heat of the compressor shaft power x mechanical efficiency x (1-adiabatic efficiency) passes through the compressor.
  • the temperature rises by transferring heat to the steam.
  • Part of the gas that has passed through the compressor is circulated through the line 6 to the suction side of the compressor, and if the circulation continues, there is a risk that the temperature will exceed the upper limit of the compressor, so the operating condition of the compressor 5 is stable.
  • the flow control valve 12 is closed, the flow control valve 11 is kept fully open, and the process steam is started to be returned to the pipe connection portion 10 of the main process by the first circulation line 9.
  • the process steam basically passes through the compressor only once, so the temperature rise at that time is only the heat transfer from the compressor, and the temperature rise is small. Furthermore, since the temperature difference between the recompressed steam that has passed through the screw-type compressor 5 and the boiling point of the internal process of the heat exchanger 7 is not sufficient, heat transfer is insufficient and condensation does not occur so much.
  • the vapor is returned to the main process through the first circulation line 9 while remaining uncondensed.
  • the uncondensed steam can be returned to the main process by the first circulation line 9 immediately after switching to the VRC process in this way, unlike the conventional VRC system, the second circulation line 6 is circulated.
  • the flow control valve 13 is opened when the gas-liquid separator 8 confirms the liquid level of the condensate, the line is sealed, and the condensate is sent to the subsequent process.
  • the compression ratio in the compressor 5 is controlled by adjusting the opening degree.
  • the process steam (recompressed steam) compressed by the compressor 5 is designed so as to be totally condensed by the heat exchanger 7 as a heat source.
  • the non-condensable gas leaks into the process from a bearing of the compressor.
  • the steam that cannot be completely dissolved in the process condensate is separated as a gas component by the gas-liquid separator 8 and returned to the main process via the first circulation line 9 to be processed.
  • the process fluid that has returned to the connection unit 10 is usually cooled and condensed by the second condenser 3 on the downstream side of the connection unit 10, but even if it flows into the compressor side (upstream side) for some reason, the first condenser 2 is cooled and condensed at 2, so that even if it merges with the process steam discharged from the distillation column 1, the gas flow rate becomes excessive for the processes after the condensation process of the main process and the steam recompression process of the VRC process. Absent.
  • the flow control valve is adjusted to a predetermined opening before starting the compressor (if the discharge pressure of the compressor is too low, the flow control is performed in advance.
  • the flow rate of the process steam introduced into the compressor is adjusted by closing the valves 11 and / or 12), and a screw type compressor that closes the flow control valve 12 after pressurization and before pressurization is provided.
  • the process steam circulation method is different from the plant.
  • uncondensed steam can be returned to the main process through the first circulation line in the VRC process, so that the retention of process steam due to poor heat transfer in the heat exchange unit is suppressed. It is possible to prevent the compressor from being damaged due to the stagnation of the gas flow in the compressor.
  • the circulation method before the start of condensation differs depending on the type of the compressor, in any compressor, the recompressed steam can be safely and easily reused as a heat source.
  • the second circulation line 6 is used to secure a circulation flow rate in order to avoid surging in an emergency in addition to controlling the process steam circulation method.
  • a condenser capable of cooling and condensing the generated process steam is provided on the main process line, and a part of the generated process steam is compressed. Gas components separated by the gas-liquid separator, regardless of whether or not the obtained high-temperature compressed gas is used as a heat medium in the VRC process to obtain a higher-temperature gas by introducing adiabatic compression into By returning to the main process, the safety of the compressor, the flexibility of design and operation, and the controllability can be improved.
  • the process steam generator is not limited to a distillation column as long as process steam is generated.
  • the process steam generator is a device whose temperature is controlled by heating and evaporating with a heat source and then cooling and circulating.
  • it may be a reactor, an evaporator, a crystallizer, a dryer, or the like.
  • a distillation column is preferable because the VRC process is easily incorporated into the heat source of the main process.
  • the distillation tower is provided with a condenser for discharging process steam from the top of the tower and cooling and condensing the process steam, and a reboiler for gas charging of the raw material at the bottom of the distillation tower.
  • the evaporator may be used as a heat source in combination with the reboiler at the bottom of the tower.
  • the process steam may be a condensable gas and usually contains water and / or an organic solvent.
  • the organic solvent include alcohols (alkyl alcohols such as ethanol, propanol and isopropanol, glycols such as ethylene glycol and propylene glycol), esters (methyl acetate, ethyl acetate, butyl acetate and the like), ketones ( Acetone, ethyl methyl ketone, methyl isobutyl ketone, cyclohexanone, etc.), aldehydes (acetaldehyde, propionaldehyde, etc.), carboxylic acids (acetic acid, propionic acid, etc.), ethers (chain ethers such as dimethyl ether and diethyl ether, dioxane, Cyclic ethers such as tetrahydrofuran), hydrocarbons (aliphatic hydrocarbons such as hexane, alicyclic hydrocarbons such as cyclohex
  • the boiling point of the organic solvent is determined by the type of the organic solvent, but is not particularly limited, and is, for example, about 30 to 150 ° C., preferably 50 to 120 ° C., more preferably about 60 to 100 ° C.
  • the vapor pressure (25 ° C.) of the organic solvent is determined by the type of the organic solvent, but is not particularly limited, and is, for example, about 1 to 30 kPa, preferably 5 to 20 kPa, and more preferably about 10 to 15 kPa. .
  • the proportion of the organic solvent can be selected according to the type of the organic solvent and is not particularly limited, but may be 10% by weight or more, for example, 30 to 99% by weight, preferably 50 to It may be about 98% by weight, more preferably about 80 to 95% by weight (particularly 85 to 93% by weight).
  • the temperature of the process vapor can be selected according to the type of condensable gas, and is not particularly limited, but is, for example, about 20 to 200 ° C., preferably 30 to 150 ° C., and more preferably about 50 to 100 ° C.
  • the pressure of the process steam may be atmospheric pressure steam or pressurized steam.
  • the flow rate of the process steam (discharge flow rate from the process steam generator) is, for example, about 0.1 to 100 m 3 / second, preferably 1 to 50 m 3 / second, and more preferably about 3 to 10 m 3 / second.
  • the condenser in the main process may be independent, but a plurality of condensers are arranged in series in order to efficiently condense the process steam and to suppress the circulation of uncondensed steam in the VRC process.
  • two capacitors may be arranged in series.
  • capacitance of a condenser is not specifically limited, Usually, the capacity
  • the condenser is provided alone, the first circulation line is connected to the upstream side of the condenser.
  • a plurality of capacitors When arranging a plurality of capacitors, a plurality of capacitors may be arranged in series, and the first circulation line may be connected upstream of the first capacitor, but downstream of the first capacitor, And a line upstream of the last capacitor (a line between adjacent capacitors, and when two capacitors are arranged in series, a line between the first capacitor and the second capacitor)
  • the plurality of condensers may be different condensers or the same condenser, but usually the first condenser alone can condense the entire amount of evaporative gas during steady operation with only the first condenser (upstream side).
  • the main process may further include a heat exchanger such as a reboiler.
  • the heat exchanger may be, for example, a main process evaporator for charging the raw material of the process steam generator in a gaseous state.
  • the main process evaporator may be a column bottom reboiler, and a heat exchanger of the VRC process may be used as this column bottom reboiler.
  • the process steam discharge line in the main process branches into a main line for cooling and condensing the process steam by the condenser and a VRC line supplied to the VRC process.
  • VRC line supplied to the VRC process flow control is performed.
  • the unit is not essential, it is preferable to arrange a flow rate control unit for controlling the flow rate of the process steam to the VRC process upstream for stable operation of the plant. Normally, the flow rate control unit gradually increases the opening degree from the closed state at the start of operation, and is adjusted to a constant opening degree (for example, fully open) during steady operation where the VRC process is stable.
  • the ratio of the process steam distributed between the main line and the VRC line can be appropriately selected according to the capacity of the compressor.
  • the ratio supplied to the VRC line is larger. At times, the entire amount of process steam may be distributed to the VRC line, but usually some of the process steam is supplied to the main line and the remainder is supplied to the VRC line.
  • the type of the vapor recompression unit is not particularly limited, and various types of compressors such as a conventional type such as a screw type, a turbo type, and a reciprocating type can be used.
  • a conventional type such as a screw type, a turbo type, and a reciprocating type
  • the screw type and the turbo type are preferable because the effect of improving safety and simplicity is great.
  • the discharge pressure of the steam recompression unit can be selected according to the type of process steam.
  • the steady-state pressure is, for example, 30 kPaG (gauge pressure) or more, preferably 40 to 200 kPaG, more preferably about 50 to 100 kPaG. .
  • the flow rate of the circulation line is adjusted by the flow rate control unit of the first circulation line, and the process steam compression ratio (discharge pressure / suction pressure) (absolute pressure) by the steam recompression unit is controlled. Adjust the temperature of the compressed steam to the desired temperature.
  • the compression ratio can be appropriately selected according to the target temperature of the recompressed steam, and is, for example, 2.0 to 4.5, preferably 3.0 to 3.5, and more preferably 3.2 to 3.3. You may adjust to a grade.
  • the discharge temperature of the steam recompression unit can be selected according to the type of process steam. For example, it is set to a discharge temperature that is, for example, 5 ° C. higher than the temperature of the process steam before being supplied to the steam recompression unit.
  • the discharge temperature may be set higher by 5 to 100 ° C., preferably 10 to 80 ° C., and more preferably 15 to 50 ° C.
  • the second circulation line (return pipe of the compressor) is not essential, but since the VRC process can be stably operated, the second recirculation line provided with the flow rate control unit is provided. May be.
  • the flow control unit In the second circulation line in the plant equipped with the screw type compressor, in the initial stage of the VRC process operation (cold start), the flow control unit is opened to circulate the process steam to the second circulation line and start the compressor operation. Sometimes it may be used only for a short period of time until the rotating part reaches a stable rotational speed.
  • a compressor having a function of a second circulation line in its mechanism is also commercially available.
  • the VRC line introduced into the compressor may further include a flow control unit in the line after joining the second circulation line.
  • the flow rate of the process steam introduced into the compressor is adjusted by adjusting the opening of the flow control unit before starting the compressor and during stable operation of the process. May be.
  • the recompressed steam is a process steam that has passed through a steam recompression unit (process). Steam) is also referred to as recompressed steam.
  • the heat exchange unit As the heat exchange unit, a conventional heat exchanger can be used. As described above, when the heat exchange unit is used as the main process evaporator of the main process, the heat exchange unit can be used as a heat source of the main process. It can be equipment. When the heat exchange unit is used as the main process evaporator, the VRC evaporator charge amount is the total charge amount (the sum of the VRC evaporator charge amount and the main process evaporator charge amount) during steady operation of the VRC process. %) May be 50% or more, preferably 60 to 100%, more preferably about 70 to 100%. The method according to the present invention is operated by appropriately reducing the amount charged in the main process evaporator as the amount of evaporation in the heat exchange unit increases.
  • the heat exchange unit is connected to the first circulation line, and the gas component that has not been condensed in the heat exchange unit is returned to the main process by the first circulation line.
  • the heat exchange unit heat exchange step
  • the main process is performed by the first circulation line while most of the process fluid remains in the gaseous state Returned to
  • the steam recompression unit is stable, it is preferable to design the heat exchange step (efficiency) in the heat exchange unit so that all of the recompression steam is condensed.
  • the heat exchange process designed in this way since most of the recompressed steam is condensed, almost no uncondensed steam is supplied to the first circulation line.
  • gas-liquid separation unit is not essential, it is possible to improve the energy efficiency of the plant by returning the separated gas components to the main unit, so that the gas-liquid separation for gas-liquid separation of the process fluid that has passed through the heat exchange unit is possible.
  • a separator is preferably provided.
  • the gas-liquid separator is not particularly limited as long as the gas component and the condensate can be separated, and a conventional separation drum or the like can be used.
  • the amount of sealing gas such as nitrogen gas
  • the condensate is recovered from the discharge line.
  • the discharge line may not include the flow rate control unit, but it is preferable to include the flow rate control unit from the viewpoint that the VRC process can be stably operated.
  • FIG. 2 shows a process flow diagram.
  • the main process includes a distillation column 1, and the charged liquid is evaporated by a main process evaporator (first heat exchanger) 14 and charged into the distillation column 1 in a gas state.
  • the process vapor discharged from the top of the distillation column 1 is atmospheric pressure (atmospheric pressure)
  • the temperature is about 80 ° C.
  • the composition is 60% by weight of ethyl acetate, benzene
  • the flow rate is 4 m 3 / sec at 30 wt% and 10 wt% water.
  • a screw type compressor (“KS40” manufactured by Kobe Steel) was used as KS40” manufactured by Kobe Steel.
  • valve 15 of the line from the top of the distillation column 1 to the VRC process side was gradually opened to replace the VRC process line with process steam, and the temperature of the system was raised over about 10 minutes.
  • the compressor 5 was started and it was confirmed that the discharge pressure increase of the compressor was kept below 50 kPaG. After the rotor reached the rated speed (after about 10 to 20 seconds), it was confirmed that there was no abnormality (abnormal noise, vibration, etc.) in the compressor under steady continuous operation. At this time, the shaft power of the compressor 5 was 250 kW, the suction gas flow rate was 3 m 3 / sec, and the discharge gas temperature of the compressor was increased by 20 ° C. from the inlet temperature.
  • valve 11 When the operation is stable, the valve 11 is opened and closed intermittently with a small opening, and a gas mainly composed of a small amount of compressor shaft seal gas (nitrogen) leaking into the system is flowed to the main process side. Processed.
  • FIG. 3 shows a process flow diagram.
  • the plant shown in FIG. 3 is a plant having a conventional VRC process that does not include the circulation line 9 and the gas-liquid separator 8 in the plant shown in FIG.
  • the operation was performed in the same manner as in Example 1.
  • process steam was introduced into the same screw type compressor as in Example 1, the temperature increased by 20 ° C. in one pass.
  • the process steam which was 80 ° C. when introduced into the VRC process, is designed for the compressor inlet gas temperature in about 40 seconds. In order to reach the upper limit of 160 ° C., it was inevitable to stop to protect the equipment before confirming whether there was any abnormality in the compressor operating status.
  • Comparative Example 2 In the plant of Comparative Example 1, in order to suppress the rise in the compressor inlet temperature only by the operation of the second circulation line until the confirmation of the presence or absence of the operation abnormality of the compressor is completed, the same system as in Example 1 is used. In addition, a 220 kW class gas cooler with a required heat removal amount during no-load operation must be installed in the second circulation line 6 only for use at the time of start-up, resulting in excessive equipment costs.
  • FIG. 4 shows a process flow diagram.
  • the main process includes a distillation column 1, and the charged liquid is evaporated by a main process evaporator (first heat exchanger) 14 and charged into the distillation column 1 in a gas state.
  • the process vapor discharged from the top of the distillation column 1 is atmospheric pressure (atmospheric pressure)
  • the temperature is about 80 ° C.
  • the composition is 60% by weight of ethyl acetate, benzene
  • the flow rate is 4 m 3 / sec at 30 wt% and 10 wt% water.
  • a turbo compressor (“f44C2” manufactured by IHI Corporation) was used.
  • valve 15 of the line from the top of the distillation column 1 to the VRC process side was gradually opened to replace the VRC process line with process steam, and the temperature of the system was raised over about 10 minutes.
  • the valve 12 was fully closed and the valve 17 was set to a predetermined opening.
  • the compressor 5 was started and it was confirmed that the discharge pressure increase of the compressor was kept below 50 kPaG. After the impeller reached the rated speed (after about 10 to 20 seconds), it was confirmed that there was no abnormality (abnormal noise, vibration, etc.) in the compressor under steady continuous operation. At this time, the shaft power of the compressor 5 was 250 kW, the suction gas flow rate was 3 m 3 / sec, and the discharge gas temperature of the compressor was increased by 20 ° C. from the inlet temperature.
  • valve 11 When the operation is stable, the valve 11 is opened and closed intermittently with a small opening, and a gas mainly composed of a small amount of compressor shaft seal gas (nitrogen) leaking into the system is flowed to the main process side. Processed.
  • FIG. 5 shows a process flow diagram.
  • the plant shown in FIG. 5 is a plant having a conventional VRC process that does not include the circulation line 9 and the gas-liquid separator 8 in the plant shown in FIG. 4.
  • the operation was started in the same manner as in Example 2 as follows.
  • valve 15 of the line from the top of the distillation column 1 to the VRC process side was gradually opened to replace the VRC process line with process steam, and the temperature of the system was raised over about 10 minutes.
  • the valve 12 was fully closed and the valve 17 was set to a predetermined opening.
  • the method of using recompressed steam of the present invention can be used in various plants that generate process steam, such as distillation plants.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne une usine destinée à utiliser une vapeur recomprimée comprenant : une unité principale comportant un équipement (1) de génération de vapeur générant une vapeur de traitement, laquelle est un gaz condensable, et un condenseur destiné à refroidir et à condenser une partie de la vapeur de traitement qui a été générée ; une unité (5) de recompression de vapeur destinée à réaliser une compression adiabatique d'au moins une partie de la vapeur de traitement, par augmentation de la température, et ainsi obtenir une vapeur recomprimée ; et une unité (7) d'échangeur de chaleur destinée à utiliser la vapeur recomprimée comme source de chaleur. L'invention concerne également une conduite (9) de circulation destinée à renvoyer vers l'unité principale des constituants de gaz non condensés dans la vapeur recomprimée, laquelle est alimentée vers l'unité d'échangeur de chaleur. L'unité principale est pourvue d'un premier condenseur (2) et d'un second condenseur (3) du côté aval du premier condenseur, et la conduite (9) de circulation peut être reliée à une conduite entre le premier condenseur et le second condenseur. Dans cette usine, une vapeur de traitement, dont la température a été augmentée par compression adiabatique, peut être réutilisée comme source de chaleur simplement et en toute sécurité.
PCT/JP2014/073086 2013-09-06 2014-09-02 Procédé et usine pour l'utilisation de vapeur recomprimée WO2015033935A1 (fr)

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CN105669362A (zh) * 2016-03-14 2016-06-15 江苏乐科节能科技股份有限公司 三氯甲烷溶剂回收热泵精馏工艺
CN105693460A (zh) * 2016-03-14 2016-06-22 江苏乐科节能科技股份有限公司 二氯甲烷溶剂回收热泵精馏工艺
JP2017064588A (ja) * 2015-09-28 2017-04-06 株式会社ダイセル 再圧縮蒸気の利用方法及びプラント
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JP2020522376A (ja) * 2017-06-08 2020-07-30 エルジー・ケム・リミテッド 蒸留装置および蒸留方法
WO2024048724A1 (fr) * 2022-09-02 2024-03-07 東洋エンジニアリング株式会社 Dispositif de distillation et procédé de distillation

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WO2017057191A1 (fr) * 2015-09-28 2017-04-06 株式会社ダイセル Procédé et installation pour l'utilisation de vapeur recomprimée
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CN105669412A (zh) * 2016-03-14 2016-06-15 江苏乐科节能科技股份有限公司 丙酮溶剂回收热泵精馏工艺
CN105669362A (zh) * 2016-03-14 2016-06-15 江苏乐科节能科技股份有限公司 三氯甲烷溶剂回收热泵精馏工艺
CN105693460A (zh) * 2016-03-14 2016-06-22 江苏乐科节能科技股份有限公司 二氯甲烷溶剂回收热泵精馏工艺
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JP2020522376A (ja) * 2017-06-08 2020-07-30 エルジー・ケム・リミテッド 蒸留装置および蒸留方法
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WO2024048724A1 (fr) * 2022-09-02 2024-03-07 東洋エンジニアリング株式会社 Dispositif de distillation et procédé de distillation

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