CN105517682A - Method and plant for using recompressed vapor - Google Patents
Method and plant for using recompressed vapor Download PDFInfo
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- CN105517682A CN105517682A CN201480049180.0A CN201480049180A CN105517682A CN 105517682 A CN105517682 A CN 105517682A CN 201480049180 A CN201480049180 A CN 201480049180A CN 105517682 A CN105517682 A CN 105517682A
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/28—Evaporating with vapour compression
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Abstract
A plant for using recompressed vapor is provided with: a main unit having vapor generating equipment (1) that generates process vapor, which is a condensable gas, and a condenser for cooling and condensing part of the process vapor that has been generated; a vapor recompression unit (5) for carrying out adiabatic compression of at least part of the process vapor, increasing temperature, and thereby obtaining recompressed vapor; and a heat exchanger unit (7) for using the recompressed vapor as a heat source. A circulating line (9) for returning uncondensed gas components in the recompressed vapor, which is supplied to the heat exchanger unit, to the main unit is provided. The main unit is provided with a first condenser (2) and a second condenser (3) on the downstream side of the first condenser, and the circulation line (9) may be connected to a line between the first condenser and the second condenser. In this plant, process vapor which has been increased in temperature by adiabatic compression can be safely and simply reused as a heat source.
Description
Technical field
The present invention relates to the method utilizing recompression steam and the complete set of equipments using the method, the method for described utilization recompression steam is in the technique produced with steam, utilizes compressor to described steam adiabatic compression, and recycles with it can be used as heat source high-efficiency.
Background technology
Adding in the chemical technology along with the unit operation of gas-liquid phase transition, is useful thing as technique object at the process steam produced, or when containing the material be not suitable for air release, needs cooling and condensation, carries out the operation that reclaims.All the time, in this chemical technology, be designed with by process steam self is used as thermal source, realize the energy-conservation various methods of technique entirety.But these process steam temperature are low substantially, therefore for this Application way, often rest on the thermal source of the different operations low as temperature by the method for cascade or be incubated and this restrictive situation of preheating.
Vapo r recompression (VRC) mode is by using compressor to carry out adiabatic compression with the technology making temperature increase in the gas phase process comprising steam.For the compressed vapour utilizing this technology and temperature to rise, have studied the situation of thermal source its latent heat or sensible heat being used as evaporation or distillation, dry this operation.
When like this VRC mode being applied in technique, when operating beginning (cold start-up), sometimes be the uncreated situation of process steam self to compressor supply, therefore need to possess the common thermal source such as electric heater or steam boiler in addition and produce source as the process steam used when equipment operation starts.Be main technique by now on-stream original technique, and when the technique (VRC technique) of its additional VRC mode is applied, also considering to retain and utilize the process steam belonging to existing equipment to produce equipment.In a word, be in most cases adopt following commissioning steps, that is, in main technique, produce process steam, in the stage reaching stable running, process steam is distributed and imports VRC technique, implement adiabatic compression and make temperature increase, and switch thermal source.
But there is the restriction should observed according to the viewpoint of proterctive equipment in the compressor as the nucleus equipment of VRC technique, this liquid container has the one side being difficult to the application carrying out VRC in utilization.Compressor usually no matter any form, is all set with higher limit to application of temperature.Such as, when screw, the gap turn narrow of female rotor and male rotor along with thermal expansion, therefore reaches contact, breakage to prevent, and is set with higher limit to the inlet temperature of gas.Therefore, when gas inlet temperature exceedes higher limit, have in order to proterctive equipment shut down.In order to suppress the rising of gas inlet temperature, need cooler, cost of equipment increases.In addition, in turbine type, sometimes in the equipment of target of supplying gas taking Compressed Gas as thermal source, the bad grade of heat conduction occur and condensation do not occur, thus process gas is detained.In this case, because not continuing from compressor a variety of causes such as supplying gas, the suction gas to compressor extremely reduces or interrupts, and the circulation of the gas thus in compressor is stagnated and produced surge, and easy generation equipment is damaged.The possibility particularly occurred when thermal source being switched to VRC technique to the damaged relevant unfavorable condition of these equipment is high, needs to implement in technique for guaranteeing some safe process, but not yet proposes effective process.
Such as, following method is disclosed in Japan Patent No. 3221695 publication (patent document 1), passing through heat pump mode (vapo r recompression mode) from the method for the stoste recycling design containing nonvolatile matter, steam is imported to Pistonless compressor from the tower top pipeline of heat pump distillation tower, after boosting, heating up, reboiler is utilized to provide required heat to described destilling tower.
But, in the publication, have the record of scheme about technological process and energy-saving effect, but the improvement of the technique for the viewpoint for equipment protection as above do not recorded.
Prior art document
Patent document
Patent document 1:(Japan) patent No. 3221695 publication (claims, [0002] section [0006] section, Fig. 1)
Summary of the invention
Invent problem to be solved
Therefore, the object of the present invention is to provide the process steam safety temperature by adiabatic compression risen and easily as thermal source recycling method and use the complete set of equipments of the method.
For solving the means of problem
The present inventor furthers investigate for realizing described problem, found that, will to process steam adiabatic compression (vapo r recompression; VRC) the recompression steam obtained is used as in the method for thermal source, by make in the recompression steam of heat exchange operation supply, uncooled gas componant returns main technique (master operation), using process steam (recompression steam) safety of the temperature rising by adiabatic compression and easily as thermal source recycling, thus the present invention can be completed.
That is, the method for recompression steam that utilizes of the present invention comprises: produce the process steam as condensing gas, and the process steam of generation is formed as the master operation that condensate liquid carries out reclaiming; At least partially adiabatic compression of compressor to described process steam is utilized to make temperature increase and obtain recompressing the vapo r recompression operation of steam; Recompression steam is used as the heat exchange operation of thermal source; Make in the recompression steam supplied to heat exchange operation, that uncooled gas componant returns master operation circulating process.At described master operation, such as, the part cooling also condensation of the process steam of generation can be made, and in described vapo r recompression operation, utilize the remainder adiabatic compression of compressor to described process steam to make temperature increase, and obtain recompressing steam.In described master operation, after the process fluid that can obtain making condensation process steam and the gas componant from circulating process are collaborated, make the mixture cooling also condensation at interflow.Method of the present invention can also comprise the gas-liquid separation operation for making the process fluid gas-liquid separation through heat exchange operation, in circulating process, makes isolated gas componant in described gas-liquid separation operation return master operation.In described circulating process, also can be returned the flow of the gas componant of (circulation) master operation by adjustment, control the compression ratio in vapo r recompression operation.Described master operation also can comprise distillation process.In described heat exchange operation, also recompression steam can be used as the thermal source of master operation.
Also comprise the complete set of equipments utilizing recompression steam in the present invention, it possesses: have and produce as the vapor generator of the process steam of condensing gas and for making a part for the process steam of generation cool and the master unit of the condenser of condensation; The vapo r recompression unit recompressing steam is obtained for making temperature rise to the remainder adiabatic compression of described process steam; For recompression steam being used as the heat exchange unit of thermal source; For make in the recompression steam of heat exchange unit supply, uncooled gas componant returns the circulation line of master unit.The condenser (independent condenser) that described master unit can possess the discharge line for discharging process steam and be connected with this discharge line, described discharge line is branched off into for a part for process steam being supplied to the pipeline of described condenser and being used for remainder to be supplied to the pipeline of vapo r recompression unit, and circulation line is connected with the pipeline of the condenser upstream side of master unit.In addition, master unit also can be possessed the discharge line for discharging process steam and be connected and the multiple condensers configured successively by pipeline, described discharge line is branched off into for a part for process steam being supplied to the pipeline of first condenser and being used for remainder to be supplied to the pipeline of vapo r recompression unit, and first condenser downstream side of circulation line and master unit and the pipeline of last condenser upstream side are connected.Complete set of equipments of the present invention can also possess for making the process fluid gas-liquid separation through heat exchange unit and making isolated gas componant return the gas-liquid separation unit of master unit.Also the flow controlling unit that the flow that can be returned the gas componant of (circulation) master unit by adjustment adjusts the compression ratio in vapo r recompression unit can be equipped in described circulation line.Described master unit can also comprise destilling tower.In described heat exchange unit, also recompression steam can be used as the thermal source of master unit.
In addition, in this manual, " process steam " refers to and is adding the steam produced in the manufacturing process (operation) with the unit operation of gas-liquid phase transition, " recompression steam " refers in vapo r recompression mode (VRC), in order to be used as the process steam that thermal source makes temperature rise by adiabatic compression.
Invention effect
In the present invention, in VRC technique, make in the recompression steam of heat exchange operation supply, uncooled gas componant returns main technique (master operation), therefore, it is possible to recompression steam is safe and recycle easily as thermal source.Particularly in the equipment that resource-saving is energy-saving, recompression steam can be used as thermal source, the Application way that design and the flexibility operated and controlling can be provided all excellent and complete set of equipments, specifically, in screw compressor, also the excessive rising of gas inlet temperature can be suppressed after thermal source is switched to VRC technique, do not need cooling device, and in turbocompressor, the delay etc. of the process steam that the heat conduction in heat exchange unit also can be suppressed bad etc. to cause, the breakage of the compressor that the stagnation etc. that can prevent the gas in compressor from circulating causes.
Accompanying drawing explanation
Fig. 1 is for illustration of the process chart utilizing the recompression method of steam and an example of complete set of equipments (device) of the present invention.
Fig. 2 is the utilization recompression method of steam and the process chart of device for illustration of embodiment 1.
Fig. 3 is the utilization recompression method of steam and the process chart of device for illustration of comparative example 1.
Fig. 4 is the utilization recompression method of steam and the process chart of device for illustration of embodiment 2.
Fig. 5 is the utilization recompression method of steam and the process chart of device for illustration of comparative example 3.
Detailed description of the invention
Below, as required, the present invention is illustrated in greater detail with reference to accompanying drawing.
In the example of Fig. 1, the complete set of equipments of utilization recompression steam possesses the destilling tower 1 as process steam maker, this process steam maker is discharged as the process steam of condensing gas, and for discharge process steam from this destilling tower 1 discharge line in branch point 4 branch.Being equipped for making a part for the process steam of discharging from destilling tower 1 cool and the first condenser 2 and the second condenser 3 of condensation at the pipeline of the side branched out, utilizing condenser cooled by above-mentioned process steam and form condensate liquid to reclaim.Master unit comprises described destilling tower 1 and the first condenser 2 and the second condenser 3.
In addition, be equipped in the pipeline of the opposing party of branch: as the screw compressor 5 of vapo r recompression unit, it makes temperature rise to the remainder adiabatic compression of the described process steam of the pipeline via the flow control valve (valve) 15 be equipped as flow controlling unit and obtains recompressing steam; As the heat exchanger 7 of heat exchange unit, it is used as thermal source for recompressing steam; As the gas-liquid separator 8 of gas-liquid separation unit, it for making the process fluid gas-liquid separation through over-heat-exchanger 7, and makes isolated gas componant return master unit.In this gas-liquid separator 8, the process fluid through over-heat-exchanger 7 is separated into further gas componant and liquid component (condensate liquid), isolated condensate liquid is recovered from the pipeline possessed as the flow control valve 13 of flow controlling unit.On the other hand, in gas-liquid separator 8, isolated gas componant returns master unit by the first circulation line 9 together with the gas of the gas circuit from above-mentioned heat exchanger 7.The pipeline that this first circulation line 9 is connected between the first condenser 2 and the second condenser 3 via connecting portion 10, collaborates with by the process fluid of the first condenser 2, and in the second condenser cooling condensation and being recovered.And, in described screw compressor 5, also can arrange the second circulation line 6 of being linked by the pipeline of the pipeline of the entrance side of compressor and outlet side and the flow control valve 12 as flow controlling unit.
In addition, Application way of the present invention or complete set of equipments are divided into master operation (main technique) and VRC operation (VRC technique), in described master operation, comprise destilling tower 1 and the first condenser 2, and comprise the second condenser 3 as required, produce the process steam as condensing gas, make it cool and condensation; In VRC operation, comprise screw compressor 5, heat exchanger 7 and gas-liquid separator 8, utilize compressor make temperature increase to process steam adiabatic compression and generate recompression steam, and used as thermal source.In addition, in this manual, in Fig. 2 ~ 5, for the inscape identical with Fig. 1, identical Reference numeral is added.
In the complete set of equipments (device) with this structure, before VRC operation starts, operate by means of only master operation.That is, flow control valve 15 cuts out, and from process steam all cooling condensations the first condenser 2 and the second condenser 3 that destilling tower 1 is discharged, forms condensate liquid and be recovered.Then, flow control valve 11,12,15 is being opened completely and under the state that flow control valve 13 cuts out, is starting screw compressor 5, make it be stabilized in rated speed.Now, from destilling tower 1 discharge process steam a part through the discharge line of master operation branch point 4 and be sucked into compressor 5 side, replace with the sealing gas of the pipeline in VRC operation.Now, ejection pressure is not almost applied to the process steam by screw compressor 5, but is delivered to by the process steam in compressor by the heat of shaft power × mechanical efficiency × (the 1-adiabatic efficiency) of compressor, and occurrence temperature rises.Be recycled to the suction side of compressor by pipeline 6 by the part of the gas of compressor, if circulation continuous, then likely reach the high temperature higher than the compressor upper limit, therefore after the operating condition of compressor 5 is stable, flow control valve 12 cuts out, and make flow control valve 11 keep opening completely, process steam is begun through tubing connection portion 10 that the first circulation line 9 returns master operation.Now, process steam substantially only by compressor once, therefore temperature at this moment rises just from the heat conduction of compressor, and temperature ascensional range is little.And, also not enough by the temperature difference of the boiling point of the temperature of the recompression steam of screw compressor 5 and the internal process of heat exchanger 7, therefore heat conduction is also insufficient, hardly condensation occurs, and most process steam returns master operation via the first circulation line 9 under the uncooled state of maintenance.In the present invention, after switching to VRC operation like this, the first circulation line 9 can be utilized to make uncooled steam return master operation, therefore different from existing VRC mode, before because circulating in the second circulation line 6, compressor is heated to more than ceiling temperature, stop at the circulation in the second circulation line 6, uncooled steam can be discharged to the first circulation line from heat exchanger 7.Therefore, the equipment that the compressor that there is no need for heating up to the circulation because of the second circulation line cools.What deserves to be explained is, when confirming the liquid level of condensate liquid in gas-liquid separator 8, pipeline by fluid-tight, and opens flow control valve 13 to the moment of operation transport of condensate afterwards.
Then, flow control valve 11 cuts out gradually, the ejection pressure of compressor 5 is increased gradually, is then risen by the temperature of the process steam compressed, but in order to the temperature of regulation can be maintained, controlled the compression ratio in compressor 5 by the aperture adjustment of flow control valve 11.To the process steam compressed by compressor 5 (recompression steam) to carry out technological design as the mode of thermal source total condensation in heat exchanger 7, but in the non-condensing gas that the bearing etc. from compressor bleeds in technique, the steam that is not dissolved in process condensate, be separated by gas-liquid separator 8 as gas componant, and return main technique via the first circulation line 9, process.Return the process fluid cooling condensation in second condenser 3 in connecting portion 10 downstream usually of connecting portion 10, even if but because of some reason inflow compressor side (upstream side), also can in the first condenser 2 cooling condensation, even if therefore collaborate with the process steam of discharging from destilling tower 1, for the condensation procedure of main technique and the later operation of the vapo r recompression operation of VRC operation, gas flow also can not be excessive.
What deserves to be explained is, in FIG, the method of recompression steam is utilized to be illustrated to the complete set of equipments by possessing screw compressor, but in the complete set of equipments possessing turbocompressor, before compressor boosting starts (condensation start before) VRC technique in the round-robin method of process steam slightly different.Specifically, in the complete set of equipments possessing turbocompressor, as the device forming complete set of equipments, not only the kind of compressor is different, and possess in flow control valve this point in the pipeline (pipeline after collaborating with the second circulation line 6) of entrance side at compressor, different from the complete set of equipments possessing screw compressor.Therefore, in the complete set of equipments possessing turbocompressor, before startup compressor, by described flow control valve being adjusted to the aperture of regulation (when the ejection of compressor presses through low, close flow control valve 11 and/or 12 in advance), adjust the flow of the process steam importing compressor, and after the startup of compressor, the round-robin method of process steam is different from the complete set of equipments possessing screw compressor of being closed by flow control valve 12 before boosting.In the complete set of equipments possessing turbocompressor, the first circulation line can be utilized in VRC operation to make uncooled steam return master operation, therefore, it is possible to the delay etc. of heat conduction in the suppression heat exchange unit process steam caused such as bad, the breakage of the compressor that the stagnation etc. that can prevent the gas in compressor from circulating causes.Like this, although according to the kind of compressor condensation start before round-robin method different, recompression steam can both be recycled easily as thermal source safety in any compressor.What deserves to be explained is, in the complete set of equipments possessing turbocompressor, the second circulation line 6, except the control of the round-robin method of process steam, is also used in the surge avoiding emergency, guarantees circular flow.
Utilize in the method (or equipment) of recompression steam of the present invention, the pipeline of master operation possesses and can make the process steam cooling condensation of generation and carry out the condenser that reclaims, and carrying out adiabatic compression at the part importing compressor by the process steam by generation is formed in the VRC operation of gas at higher temperature, no matter whether the Compressed Gas of obtained high temperature is effectively utilized as thermal medium, all master operation is returned for gas componant isolated in gas-liquid separator, security and the design of compressor can be improved thus, the flexibility of running, controlling.
In master operation (master unit), as long as process steam maker produces process steam, then be not limited to destilling tower, such as, also can be carry out temperature controlled device by cool cycles after being evaporated by heat source, specifically, also can be reactor, evaporimeter, crystallizer, drying machine etc.Wherein, from easy thermal source this point VRC operation being added master operation, preferably destilling tower.Destilling tower discharges process steam from tower top, possess and make the condenser of this process steam cooling condensation and the reboiler for inserting raw material at the bottom of tower with gas shape, and also can, using the heat exchanger of VRC operation (VRC evaporimeter) as thermal source, come to use in the lump with the reboiler at the bottom of above-mentioned tower.
As long as process steam condensing gas, usually containing water and/or organic solvent.As organic solvent, such as alcohols (ethanol can be enumerated, propyl alcohol, the alkanols such as isopropyl alcohol, ethylene glycol, the glycols etc. such as propane diols), ester class (methyl acetate, ethyl acetate, butyl acetate etc.), ketone (acetone, ethyl methyl ketone, hexone, cyclohexanone etc.), aldehydes (acetaldehyde, propionic aldehyde etc.), carboxylic acids (acetic acid, propionic acid etc.), ethers (dimethyl ether, the chain ethers such as Anaesthetie Ether, diox, the ring-type ethers etc. such as oxolane), hydro carbons (the aliphatic hydrocarbon such as hexane, the ester ring type hydro carbons such as cyclohexane, benzene, toluene, the arenes etc. such as dimethylbenzene), halogenated hydrocarbon (carrene, chloroform etc.) etc.These organic solvents can two or more use alone or in combination.In these organic solvents, general ester class (particularly acetic acid esters), hydro carbons (particularly aromatic hydrocarbon based), also can such as with ester class/hydrocarbon=99/1 ~ 10/90, preferably 90/10 ~ 30/70, more preferably about 80/20 ~ 50/50 part by weight mixed ester class and hydro carbons.
The boiling point of organic solvent determines according to the kind of organic solvent, but is not particularly limited, and such as, is 30 ~ 150 DEG C, is preferably 50 ~ 120 DEG C, is more preferably about 60 ~ 100 DEG C.
The vapour pressure (25 DEG C) of organic solvent determines according to the kind of organic solvent, but is not particularly limited, and such as, is 1 ~ 30kPa, is preferably 5 ~ 20kPa, is more preferably about 10 ~ 15kPa.
The ratio of organic solvent can be selected according to the kind of organic solvent, be not particularly limited, but it is overall relative to process steam, can be more than 10 % by weight, such as 30 ~ 99 % by weight, being preferably 50 ~ 98 % by weight, more preferably can be 80 ~ 95 % by weight (particularly 85 ~ 93 % by weight) left and right.
The temperature of process steam can be selected according to the kind of condensing gas, is not particularly limited, but is such as 20 ~ 200 DEG C, is preferably 30 ~ 150 DEG C, is more preferably about 50 ~ 100 DEG C.The steam of process steam can be pressure be normal pressure also can be pressurized steam.The flow (delivery flow from process steam maker) of process steam is such as 0.1 ~ 100m
3/ second, be preferably 1 ~ 50m
3/ second, be more preferably 3 ~ 10m
3about/second.
The condenser of master operation can be used alone, but from enabling process steam high-efficiency condensation, and suppresses uncooled steam to circulate in VRC operation this point, and preferably series connection arranges multiple condenser, such as, two condensers series connection can be arranged.The ability of condenser is not particularly limited, and usually, selects to rely on the individual operation of the master operation not making VRC operation operate just can make the ability of process steam condensation.When arranging separately condenser, the first circulation line is connected with condenser upstream side.When arranging multiple condenser, multiple condenser series connection is arranged, the first circulation line can be connected at first condenser upstream side, but pass through first condenser downstream side and the pipeline (pipeline between adjacent condenser of last condenser upstream side, in the situation of series connection arranging two condensers, pipeline between first condenser and the second condenser) connect the first circulation line, the uncooled steam from the first circulation line can be suppressed in VRC operation to circulate (adverse current).Multiple condenser can be different condenser, also can be identical condenser, but usually used as first condenser, use the condenser with boil-off gas when only relying on first (upstream side) condenser just the to make steady running ability of whole condensation as far as possible.
Master operation can also possess the heat exchangers such as reboiler.Heat exchanger can be such as the main technique evaporimeter of the raw material for inserting process steam maker with gas shape.Special when destilling tower, as above-mentioned, main technique evaporimeter can be bottom reboiler, also the heat exchanger of VRC operation can be used as this bottom reboiler.
The discharge line of the process steam in master operation is branched off into and utilizes described condenser to make the main line of process steam cooling condensation and the VRC pipeline to the supply of VRC operation, in the VRC pipeline supplied to VRC operation, flow controlling unit not necessarily, but in order to the steady running of complete set of equipments, preferably arrange in upstream and be used for the flow controlling unit of Controlling Technology steam to the flow of VRC operation.This flow controlling unit increases aperture when operating and starting from the state of closing usually gradually, is adjusted to certain aperture (such as standard-sized sheet) when the steady running that VRC operation is stable.The ratio of the process steam distributed to main line and VRC pipeline suitably can be selected according to the ability of compressor, from energy-conservation this point, ratio preferably to the supply of VRC pipeline is large, such as, when steady running, whole process steams can be assigned to VRC pipeline, but usually, part process steam is supplied to main line, and remainder is supplied to VRC pipeline.
In VRC operation, the form of vapo r recompression unit is not particularly limited, and can use conventional form, such as screw, turbine type, various types of compressor such as reciprocating.In the middle of them, from the viewpoint that the raising effect of security and simplicity is large, preferred screw, turbine type.
The ejection pressure of vapo r recompression unit can be selected according to the kind of process steam, but pressure when stablizing is such as more than 30kPaG (gauge pressure), is preferably 40 ~ 200kPaG, is more preferably about 50 ~ 100kPaG.
In the present invention, by utilizing the flow of the flow controlling unit adjustment circulation line of the first circulation line, and control the compression ratio (ejection pressure/suction pressure) (absolute pressure) of vapo r recompression unit to process steam, the temperature of recompression steam is adjusted to object temperature.In the present invention, if tighten up flow controlling unit to suppress flow, then compression ratio rises, and because of the rising of compression ratio, temperature rises, and can improve heat exchanger effectiveness thus.Described compression ratio suitably can be selected according to the object temperature of recompression steam, such as, can be adjusted to 2.0 ~ 4.5, be preferably 3.0 ~ 3.5, be more preferably adjusted to about 3.2 ~ 3.3.
The ejection temperature of vapo r recompression unit suitably can be selected according to the kind of process steam, such as, relative to the temperature to the process steam before the supply of vapo r recompression unit, such as also can be set as the height ejection temperature of more than 5 DEG C, such as, 5 ~ 100 DEG C can be set as, be preferably set to 10 ~ 80 DEG C, more preferably be set as the height ejection temperature of about 15 ~ 50 DEG C.
In vapo r recompression unit, the second circulation line (the returning pipe arrangement of compressor) not necessarily, but from making VRC operation runs steadily this point, also can possess the second circulation line being equipped with flow controlling unit.In the second circulation line in the complete set of equipments possessing screw compressor, can at VRC operation start of run (cold start-up), open flow controlling unit, process steam is circulated in the second circulation line, and uses the second circulation line in short time when the running of compressor starts only before rotating part reaches stable rotating speed.For compressor, the type in its mechanism with the function of the second circulation line commercially also has sale.And in turbocompressor, the VRC pipeline importing compressor can also possess flowing control unit in the pipeline after collaborating with the second circulation line.In the complete set of equipments possessing turbocompressor, before compressor start and in the steady running of technique, by the aperture of this flowing control unit of adjustment, the flow of the process steam importing compressor can be adjusted.
In addition, in this manual, for recompression steam, except above-mentioned definition, if have passed the process steam of vapo r recompression unit (operation), then process steam during cold start-up (degree of compression and temperature rise little steam) is also referred to as recompression steam.
Heat exchange unit can use conventional heat exchanger, as mentioned above, if be used as the main technique evaporimeter of master operation, then heat exchange unit can be used as the thermal source of master operation, therefore, it is possible to complete set of equipments to be formed as the energy-saving equipment of resource-saving.When by heat exchange unit with decide technique evaporimeter, when the steady running of VRC operation, the amount of inserting of VRC evaporimeter can be more than 50% of all amounts of inserting (total amount of the amount of inserting of VRC evaporimeter and the amount of inserting of main technique evaporimeter), be preferably 60 ~ 100%, be more preferably about 70 ~ 100%.In the method for the invention, along with the increase of the evaporation capacity of heat exchange unit, suitably the amount of inserting reduced in main technique evaporimeter operates.
Heat exchange unit is connected with the first circulation line, and the uncooled gas componant in heat exchange unit returns master operation by the first circulation line.In heat exchange unit (heat exchange operation), the start of run before vapo r recompression unit is stablized, the temperature of recompression steam rises low, and therefore most process fluid keeps gas shape to return master operation by the first circulation line.On the other hand, preferably under the stable state of vapo r recompression unit, technological design is carried out to make the heat exchange operation (efficiency) of the mode of the whole condensation of recompression steam to heat exchange unit.In the heat exchange operation of design like this, recompression steam is substantially all condensed, and therefore there is the uncooled steam to the first circulation line supply hardly.
Gas-liquid separation unit not necessarily, but can improve the energy efficiency this point of equipment from by making the gas componant of separation return master unit, preferably possesses the gas-liquid separator for making the process fluid gas-liquid separation through heat exchange unit.As gas-liquid separator, as long as can separates gas components and condensate liquid, be not particularly limited, conventional separator etc. can be utilized.
In gas-liquid separation unit, except steam uncooled in heat exchange unit, the sealing gas (nitrogen etc.) bled from the bearing etc. of compressor in technique, to be insoluble to process condensate composition is also separated as gas componant, and returns master operation by the first circulation line and process.On the other hand, condensate liquid is recovered from discharge line.
Discharge line also can not possess flow controlling unit, but from making VRC operation runs steadily this point, preferably possesses flow controlling unit.
Embodiment
Below, illustrate in greater detail the present invention based on embodiment, but the present invention can't help these embodiments limit.
(embodiment 1)
Represent process chart in fig. 2.Main technique (master operation) possesses destilling tower 1, inserts liquid and evaporates in main technique evaporimeter (the first heat exchanger) 14, and insert destilling tower 1 under gaseous state.When by means of only main process stabilizing operate time, the process steam of discharging from the tower top of destilling tower 1 is under normal pressure (atmospheric pressure), and temperature about 80 DEG C, it consists of ethyl acetate 60 % by weight, benzene 30 % by weight, water 10 % by weight, and flow is 4m
3/ second.As the compressor of VRC technique, use screw compressor ((strain) Kobe Steel made " KS40 ").
Process steam displacement ~ the compressor start of 1.VRC process pipeline ~ compressor boosting starts (condensation start before)
(1) confirm that valve 11,12,13,15 cuts out completely.
(2) valve 12 of valve 11, second circulation line of the first circulation line is opened completely.
(3) tower top from destilling tower 1 is opened gradually to the valve 15 of the pipeline of VRC technique side, in the pipeline of VRC technique, utilize process steam to replace, spend and within about 10 minutes, make temperature in system increase.
(4) start compressor 5, confirm that the ejection pressure increase of compressor is lower than 50kPaG.After rotor reaches rated speed (after about 10 ~ 20 seconds), be confirmed to be steady and continuous operating condition and do not have abnormal (abnormal sound, vibration etc.) within the compressor.The shaft power of compressor 5 is now 250kW, and suction gas flow is 3m
3/ second, the ejection gas temperature of compressor rises 20 DEG C than inlet temperature.
(5) when gradually the valve 12 of the second circulation line cuts out by (about 10 ~ 15 seconds) completely, the ejection pressure increase of compressor 5.Confirm that now ejection pressure is 50 ~ 100kPaG, ejection temperature is 97 ~ 103 DEG C.
(6) valve 11 of the first circulation line cuts out gradually.Now, the ejection pressure increase of compressor 5 is to 115kPaG.Temperature about 105 DEG C.
2. the load of boosting (condensation the starts rear) ~ existing evaporimeter of compressor reduces
(1) while observe the ejection pressure of compressor 5 and the balance of condensation, the valve 11 of the first circulation line cuts out gradually, makes ejection temperature be 110 DEG C, in VRC evaporimeter (the second heat exchanger) 7, carry out heat exchange.
(2) along with the increase of the evaporation capacity in VRC evaporimeter 7, the amount of inserting from VRC evaporimeter increases gradually.If the amount of inserting from VRC evaporimeter exceedes 70% of maximum, then under the state of minimum load keeping main technique evaporimeter 14, regulate thermal source steam 16 to the flow of main technique evaporimeter with the direction of reducing, adjustment carrys out the amount of inserting of autonomous technique evaporimeter.
(3) running stable after, make valve 11 with the opening and closing discontinuously of the aperture of trace, going forward side by side row relax with shaft seal for compressor gas (nitrogen) the main technique side of gas flow that is principal component of the intrasystem trace that makes to bleed.
(comparative example 1)
Represent process chart in figure 3.Complete set of equipments shown in Fig. 3 is the complete set of equipments possessing the existing VRC technique not possessing circulation line 9 and gas-liquid separator 8 in the complete set of equipments shown in Fig. 2.Only possessing the second circulation line as in the existing VRC technique of circulation line, implementing running in the same manner as example 1.Identically with embodiment 1 to screw compressor introducing technology steam, rise in the temperature by once realizing 20 DEG C afterwards.Relative to the capacity 30m of the second circulation line
3, take circular flow as 3m
3/ second is when operating; the process steam starting to be only when importing VRC technique 80 DEG C reached the design higher limit 160 DEG C of the gasinlet temperature of compressor at about 40 seconds; therefore, confirmation compressor operation state have without exception before, have in order to equipment protection stop.
(comparative example 2)
In the complete set of equipments of comparative example 1, before confirmation compressor is with or without running abnormal ending, rise to suppress the inlet temperature of running and compressor because only having the second circulation line, must arrange on the second circulation line 6 relative to the necessity during system no-load running identical with embodiment 1 except under heat be the gas cooler of 220kW level only to use when starting, thus cost of equipment is excessive.
(embodiment 2)
Fig. 4 represents process chart.Main technique (master operation) possesses destilling tower 1, inserts liquid and evaporates in main technique evaporimeter (the first heat exchanger) 14, insert destilling tower 1 under the state of gas.When carrying out stable running by means of only main technique, from process steam temperature about 80 DEG C under normal pressure (atmospheric pressure) that the tower top of destilling tower 1 is discharged, it consists of ethyl acetate 60 % by weight, benzene 30 % by weight, water 10 % by weight, and flow is 4m
3/ second.As the compressor of VRC technique, use turbocompressor ((strain) IHI system " f44C2 ").
The boosting of the startup ~ compressor of the process steam displacement ~ compressor of 1.VRC process pipeline starts (condensation start before)
(1) confirm that valve 11,12,13,15,17 cuts out completely.
(2) valve 12 of valve 11, second circulation line of the first circulation line, the valve 17 of compressor suction side are opened completely.
(3) tower top from destilling tower 1 is opened gradually to the valve 15 of the pipeline of VRC technique side, in the pipeline of VRC technique, utilize process steam to replace, spend and within about 10 minutes, make temperature in system increase.Valve 12 cuts out completely, and makes valve 17 become the aperture of regulation.
(4) start compressor 5, confirm that the ejection pressure increase of compressor is lower than 50kPaG.After turbine reaches rated speed (after about 10 ~ 20 seconds), be confirmed to be constant continuous operating condition and do not have abnormal (abnormal sound, vibration etc.) within the compressor.The shaft power of compressor 5 is now 250kW, and suction gas flow is 3m
3/ second, the ejection gas temperature of compressor rises 20 DEG C than inlet temperature.
(5) valve 11 of the first circulation line cuts out gradually.Now, the ejection pressure increase of compressor 5 is to 115kPaG.Temperature about 105 DEG C.
2. the load of compressor boosting (condensation starts rear) ~ existing evaporimeter reduces
(1) while observe the ejection pressure of compressor 5 and the balance of condensation, the valve 11 of the first circulation line cuts out gradually, makes ejection temperature be 110 DEG C, in VRC evaporimeter (the second heat exchanger) 7, carry out heat exchange.
(2) along with the increase of the evaporation capacity in VRC evaporimeter 7, the amount of inserting from VRC evaporimeter increases gradually.If the amount of inserting from VRC evaporimeter exceedes 70% of maximum, then under the state of minimum load keeping main technique evaporimeter 14, regulate thermal source steam 16 to the flow of main technique evaporimeter with the direction of reducing, improve the aperture of valve 17 gradually, improve the soakage of compressor, adjustment carrys out the amount of inserting of autonomous technique evaporimeter.
(3) running stable after, make valve 11 opening and closing discontinuously with the aperture of trace, going forward side by side row relax with shaft seal for compressor gas (nitrogen) the main technique side of gas flow that is principal component of the intrasystem trace that makes to bleed.
(comparative example 3)
Represent process chart in Figure 5.Complete set of equipments shown in Fig. 5 is the complete set of equipments possessing the existing VRC technique not possessing circulation line 9 and gas-liquid separator 8 in the complete set of equipments shown in Fig. 4.Only possessing the second circulation line as in the existing VRC technique of circulation line, as described below, start running in the same way as in example 2.
(1) confirm that valve 12,13,15,17 cuts out completely.
(2) valve 12 of circulation line, the valve 17 of compressor suction side are opened completely.
(3) tower top from destilling tower 1 is opened gradually to the valve 15 of the pipeline of VRC technique side, in the pipeline of VRC technique, utilize process steam to replace, spend and within about 10 minutes, make intrasystem temperature increase.Valve 12 cuts out completely, and makes valve 17 become the aperture of regulation.
(4), after starting compressor 5, at 40 seconds, the inlet temperature of compressor reached and arranges higher limit that is 160 DEG C, therefore shuts down.
Utilizability in industry
The various complete set of equipments utilizing the method for recompression steam to may be used for producing process steam of the present invention, such as, be distilled into complete equipment etc.
Description of reference numerals
1: destilling tower
2,3: condenser
4: pipe arrangement branch point
5: compressor
6,9: circulation line
7,14: heat exchanger (evaporimeter)
8: gas-liquid separator
Claims (13)
1. utilize a method for recompression steam, it is characterized in that, comprising:
Produce as the process steam of condensing gas, and the process steam of generation is formed as the master operation that condensate liquid carries out reclaiming; At least partially adiabatic compression of compressor to described process steam is utilized to make temperature increase and obtain recompressing the vapo r recompression operation of steam; Recompression steam is used as the heat exchange operation of thermal source; Make in the recompression steam supplied to heat exchange operation, that uncooled gas componant returns master operation circulating process.
2. the method for claim 1, is characterized in that,
In master operation, make condensation process steam and after the process fluid that obtains and the gas componant from circulating process collaborate, make the mixture cooling also condensation at interflow.
3. method as claimed in claim 1 or 2, is characterized in that,
Also comprising the gas-liquid separation operation for making the process fluid gas-liquid separation through heat exchange operation, in circulating process, making isolated gas componant in described gas-liquid separation operation return master operation.
4. the method according to any one of claims 1 to 3, is characterized in that,
At circulating process, returned the flow of the gas componant of master operation by adjustment, control the compression ratio in vapo r recompression operation.
5. the method according to any one of Claims 1 to 4, is characterized in that,
Master operation comprises distillation process.
6. the method according to any one of Claims 1 to 5, is characterized in that,
In heat exchange operation, recompression steam is used as the thermal source of master operation.
7. utilize a complete set of equipments for recompression steam, it is characterized in that possessing:
Have and produce as the vapor generator of the process steam of condensing gas and for making a part for the process steam of generation cool and the master unit of the condenser of condensation; The vapo r recompression unit recompressing steam is obtained for making temperature rise to the remainder adiabatic compression of described process steam; For recompression steam being used as the heat exchange unit of thermal source; For make in the recompression steam of heat exchange unit supply, uncooled gas componant returns the circulation line of master unit.
8. complete set of equipments as claimed in claim 7, is characterized in that,
The condenser that master unit possesses the discharge line for discharging process steam and is connected with this discharge line, described discharge line is branched off into for a part for process steam being supplied to the pipeline of described condenser and being used for remainder to be supplied to the pipeline of vapo r recompression unit, and circulation line is connected with the pipeline of the condenser upstream side of master unit.
9. complete set of equipments as claimed in claim 7, is characterized in that,
Master unit is possessed the discharge line for discharging process steam and is connected and the multiple condensers configured successively by pipeline, described discharge line is branched off into for a part for process steam being supplied to the pipeline of first condenser and being used for remainder to be supplied to the pipeline of vapo r recompression unit, and first condenser downstream side of circulation line and master unit and the pipeline of last condenser upstream side are connected.
10. the complete set of equipments according to any one of claim 7 ~ 9, is characterized in that,
Also possess for making the process fluid gas-liquid separation through heat exchange unit and making isolated gas componant return the gas-liquid separation unit of master unit.
11. complete set of equipments according to any one of claim 7 ~ 10, is characterized in that,
The flow controlling unit that can adjust the compression ratio in vapo r recompression unit by adjusting the flow returning the gas componant of master unit is equipped in circulation line.
12. complete set of equipments according to any one of claim 7 ~ 11, is characterized in that,
Master unit comprises destilling tower.
13. complete set of equipments according to any one of claim 7 ~ 12, is characterized in that,
In heat exchange unit, recompression steam is used as the thermal source of master unit.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2013-184738 | 2013-09-06 | ||
| JP2013184738 | 2013-09-06 | ||
| PCT/JP2014/073086 WO2015033935A1 (en) | 2013-09-06 | 2014-09-02 | Method and plant for using recompressed vapor |
Publications (2)
| Publication Number | Publication Date |
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| CN105517682A true CN105517682A (en) | 2016-04-20 |
| CN105517682B CN105517682B (en) | 2017-10-13 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480049180.0A Active CN105517682B (en) | 2013-09-06 | 2014-09-02 | Utilize the method and complete set of equipments for recompressing steam |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP6291499B2 (en) |
| CN (1) | CN105517682B (en) |
| MY (1) | MY173697A (en) |
| WO (1) | WO2015033935A1 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107758616A (en) * | 2016-08-15 | 2018-03-06 | 成都科特瑞兴科技有限公司 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
| CN107921326A (en) * | 2015-07-24 | 2018-04-17 | 森泰克有限公司 | Distilling apparatus and its distillating method |
| TWI642660B (en) * | 2017-07-19 | 2018-12-01 | 國立清華大學 | Manufacturing methods and manufacturing apparatuses of propylene carbonate and dimethyl carbonate |
| CN110449096A (en) * | 2018-05-08 | 2019-11-15 | 中国石化工程建设有限公司 | A kind of process and aromatic device low-grade utility system improving aromatic device low-grade utility efficiency |
| CN111544913A (en) * | 2020-04-27 | 2020-08-18 | 广东中科光年数智科技有限公司 | Heat pump evaporation concentration system |
| CN112169364A (en) * | 2020-09-29 | 2021-01-05 | 江苏博颂化工科技有限公司 | Fractionating tower heat pump system adopting external circulating working medium |
| CN109890476B (en) * | 2016-10-28 | 2021-09-14 | 株式会社大赛璐 | Method and plant for using recompressed steam |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6450292B2 (en) * | 2015-09-28 | 2019-01-09 | 株式会社ダイセル | Recompressed steam utilization method and plant |
| CN105669362A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Trichloromethane solvent recovery heat pump rectification process |
| CN105669412A (en) * | 2016-03-14 | 2016-06-15 | 江苏乐科节能科技股份有限公司 | Acetone solvent recovery heat-pump distillation technology |
| CN105693460A (en) * | 2016-03-14 | 2016-06-22 | 江苏乐科节能科技股份有限公司 | Heat-pump distillation technology for recycling dichloromethane solvent |
| KR102387634B1 (en) | 2017-06-08 | 2022-04-19 | 주식회사 엘지화학 | Fraction device and method for fraction thereof |
| JP2024035447A (en) * | 2022-09-02 | 2024-03-14 | 東洋エンジニアリング株式会社 | Distillation device and distillation method |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107921326A (en) * | 2015-07-24 | 2018-04-17 | 森泰克有限公司 | Distilling apparatus and its distillating method |
| CN107758616A (en) * | 2016-08-15 | 2018-03-06 | 成都科特瑞兴科技有限公司 | A kind of heat exchange of energy-conserving and environment-protective and condenser system |
| CN109890476B (en) * | 2016-10-28 | 2021-09-14 | 株式会社大赛璐 | Method and plant for using recompressed steam |
| TWI642660B (en) * | 2017-07-19 | 2018-12-01 | 國立清華大學 | Manufacturing methods and manufacturing apparatuses of propylene carbonate and dimethyl carbonate |
| CN110449096A (en) * | 2018-05-08 | 2019-11-15 | 中国石化工程建设有限公司 | A kind of process and aromatic device low-grade utility system improving aromatic device low-grade utility efficiency |
| CN111544913A (en) * | 2020-04-27 | 2020-08-18 | 广东中科光年数智科技有限公司 | Heat pump evaporation concentration system |
| CN112169364A (en) * | 2020-09-29 | 2021-01-05 | 江苏博颂化工科技有限公司 | Fractionating tower heat pump system adopting external circulating working medium |
| CN112169364B (en) * | 2020-09-29 | 2021-12-24 | 江苏博颂化工科技有限公司 | Fractionating tower heat pump system adopting external circulating working medium |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105517682B (en) | 2017-10-13 |
| JP6291499B2 (en) | 2018-03-14 |
| MY173697A (en) | 2020-02-17 |
| JPWO2015033935A1 (en) | 2017-03-02 |
| WO2015033935A1 (en) | 2015-03-12 |
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