CN105797415B - A kind of material boils module and applies its distillation system again - Google Patents
A kind of material boils module and applies its distillation system again Download PDFInfo
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- CN105797415B CN105797415B CN201410855678.8A CN201410855678A CN105797415B CN 105797415 B CN105797415 B CN 105797415B CN 201410855678 A CN201410855678 A CN 201410855678A CN 105797415 B CN105797415 B CN 105797415B
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Abstract
The present invention relates to rectifying device, discloses a kind of material and boils module again and apply its distillation system.The material boils module and included again：Vapor-liquid separation tank, Matter Transfer pipeline, Matter Transfer pump, material heater and nozzle；Liquid phase material is stored in the vapor-liquid separation tank, the charging aperture of the Matter Transfer pipeline is connected to the liquid phase material outlet of the vapor-liquid separation tank, and the discharging opening of the Matter Transfer pipeline is connected to the liquid phase material import of the vapor-liquid separation tank by the nozzle；The Matter Transfer pump is respectively arranged at the Matter Transfer pipeline with the material heater, and so that the liquid phase material is pressurized and heated, the material heater Matter Transfer pump is close to the nozzle；The liquid phase material is spurted into the vapor-liquid separation tank with so that the partial liquid phase material changes into the vapor-phase material by the nozzle.Thus, it is possible to delay or even avoid liquid phase material from boiling again in module in material cracking reaction occurs under reduced pressure atmosphere.
Description
Technical field
The present invention relates to rectifying device, more particularly to a kind of material boils module and applies its distillation system again.
Background technology
Rectifying column is a kind of tower vapor-liquid contacting apparatus for carrying out rectifying, for separate boiling point different two kinds or two kinds with
Upper mixture.Rectifying column has plate column and two kinds of main Types of packed tower, and can be divided into continuous rectifying tower according to mode of operation
With batch fractionating tower.Rectifying column is typically by tower tray (can also be packed tower), tower body, bottom of towe heater, overhead reflux line, charging
Mouth etc. is formed.Steam is entered by bottom of towe, and the gas phase evaporated carries out counter current contacting with lower descending liquid；In two are in contact, lower descending liquid
In volatile (low boiling) component constantly shifted into gas phase, difficult volatilization (higher boiling) component in gas phase is constantly downward
Shifted in descending liquid；Gas phase is closer to tower top, and its volatile components concentration is higher, and lower descending liquid is closer to bottom of towe, its difficult volatilization group
Divide concentration higher, so as to reach the purpose of component separation.The gas phase risen by tower top enters condenser, one of the liquid of condensation
It is allocated as entering in rectifying column for phegma return tower top, remaining part is then taken out as distillate.The liquid of bottom of towe outflow, its
In a part be sent into reboiler, heating evaporation into gas phase return tower in, another part liquid as kettle raffinate taking-up.
However, in the rectifying column operation of routine, often temperature is very high for tower reactor and reboiler etc., and the material in tower reactor is at this
The hot environment lower residence time is long.And thermal cracking and hot coking are easily occurring under long-time hot environment for many materials
Phenomena such as, the phenomenon is chemical reaction rather than physical reactions, so as to influence the chemical composition of rectifying product and quality etc..
The content of the invention
Module is boiled again it is an object of the invention to provide a kind of material and applies its distillation system, can be in reduced pressure atmosphere
Under delay or even avoid liquid phase material from boiling again in material cracking reaction occurs in module.
In order to solve the above technical problems, embodiments of the present invention provide a kind of material boils module again, for for rectifying
Tower provides vapor-phase material, and the material boils module and included again：Vapor-liquid separation tank, Matter Transfer pipeline, Matter Transfer pump, material add
Hot device and nozzle；Liquid phase material is stored in the vapor-liquid separation tank, the charging aperture of the Matter Transfer pipeline is connected to institute
The liquid phase material outlet of vapor-liquid separation tank is stated, the discharging opening of the Matter Transfer pipeline is connected to the vapour-liquid by the nozzle
The liquid phase material import of knockout drum；The Matter Transfer pump is respectively arranged at the Matter Transfer pipe with the material heater
Road, so that the liquid phase material is pressurized and heated, the material heater Matter Transfer pump is close to the nozzle；
The nozzle by the liquid phase material spurt into the vapor-liquid separation tank with so that the partial liquid phase material change into it is described
Vapor-phase material.
Embodiments of the present invention additionally provide a kind of distillation system, comprising：Material provided by the invention boils module again；Essence
Tower is evaporated, the bottom of towe entrance of the rectifying column is connected to the material and boils module again, and the rectifying column is used for from the vapor-phase material
In isolate vapour phase first runnings, include objective fraction in the vapour phase first runnings；Condensation module, it is connected to the tower of the rectifying column
Mouth is ejected, the condensation module distillates for condensing the vapour phase first runnings to isolate vapour phase from the vapour phase first runnings
Thing, the objective fraction is included in the vapour phase distillate；Material discharging module, it is connected to the condensation module, the material discharging module
For condensing the vapour phase distillate with so that the objective fraction is converted into target distillate.
In terms of existing technologies, material boils module and included embodiment of the present invention again：Vapor-liquid separation tank, Matter Transfer
Pipeline, Matter Transfer pump, material heater and nozzle, the Matter Transfer pump are respectively arranged at institute with the material heater
Matter Transfer pipeline is stated, so that the liquid phase material is pressurized and heated；The liquid phase material is spurted into institute by the nozzle
Vapor-liquid separation tank is stated with so that the partial liquid phase material changes into the vapor-phase material.Due to the liquid phase thing under high pressure conditions
Heat scission reaction is less likely to occur in the short time when being heated to cracking reaction temperature for material, so as to what present embodiment provided
Material boils module again can delay under reduced pressure atmosphere or even avoid liquid phase material that cracking reaction occurs in vapor-liquid separation tank.
Preferably, the material boils module and also includes material cooling tank again, is connected to the liquid phase thing of the vapor-liquid separation tank
Between material outlet and the charging aperture of the Matter Transfer pipeline, the material cooling tank is directed to after the liquid phase material is cooled down
The Matter Transfer pipeline.So as to which material cooling tank cools down to the liquid phase material in vapor-liquid separation tank, prevents liquid phase material
Cracking reaction occurs in Matter Transfer pipeline.
Preferably, the Matter Transfer pump is screw pump.So that provide the continuous liquid phase under high pressure conditions
Material.
Preferably, the condensation module includes shell-and-tube heat exchanger and heat transferring medium EGR, and the heat transferring medium follows
Loop device is connected to the shell-and-tube heat exchanger and is communicated in the shell side space of the shell-and-tube heat exchanger, the rectifying column connection
In the shell-and-tube heat exchanger and it is communicated in the tube side space of the shell-and-tube heat exchanger.So as to, by the way of infinite reflux from
Vapour phase distillate is isolated in vapour phase first runnings, the cutting accuracy being effectively improved between each fraction section, improves fractionation production
Quality.
Preferably, the material discharging module includes discharging pipeline, discharging condensing unit and collecting tank.The discharging condensation dress
Put and be located at the discharging pipeline, the thermostatted water comprising pipeline set folder, water-circulating pump and water bath with thermostatic control, the pipeline set chuck
Bath is connected to the water inlet and delivery port of the pipeline set folder, and the water-circulating pump is arranged at the water bath with thermostatic control, and the water follows
Ring pump is used to drive cooling water to circulate between the water bath with thermostatic control and pipeline set folder, to cool down in the discharging pipeline
Vapour phase distillate.It is thus possible to by controlling the temperature of cooling water come the accurate chilling temperature for controlling vapour phase distillate, Neng Goushi
Segmentation for the objective fraction with different boiling.
Brief description of the drawings
Fig. 1 is the overall schematic according to the distillation system of the better embodiment of the present invention；
Fig. 2 is the schematic diagram according to the rectifying column of the better embodiment of the present invention；
Fig. 3 is the schematic diagram for boiling module again according to the material of the better embodiment of the present invention；
Fig. 4 is the schematic diagram according to the condensation module of the better embodiment of the present invention；
Fig. 5 is the schematic diagram according to the material discharging module of the better embodiment of the present invention.
Embodiment
To make the object, technical solutions and advantages of the present invention clearer, each reality below in conjunction with accompanying drawing to the present invention
The mode of applying is explained in detail.However, it will be understood by those skilled in the art that in each embodiment of the present invention,
In order that reader more fully understands the application and proposes many ins and outs.But even if without these ins and outs and base
Many variations and modification in following embodiment, each claim of the application technical side claimed can also be realized
Case.
The better embodiment of the present invention is related to a kind of distillation system, the separation of material by the way of batch fractionating.Please one
And referring to figs. 1 to Fig. 5, distillation system 1 includes rectifying column 10, material boils module 11, condensation module 12 and material discharging module 13 again.
Wherein, the rectifying column 10 in present embodiment is packed tower, but present embodiment is not intended to be limited in any to this.
In present embodiment, rectifying column 10 includes tower body 101, packing support screen cloth 102, liquid distribution trough 103, insulation
Set 104 and filler (not shown).Specifically, tower body 101 has bottom of towe entrance 101a and tower top outlet 101b.Packing support
Screen cloth 102 is fixed on the inserts in tower body 101 and at bottom of towe entrance 101a, being filled in support in tower body 101.Liquid
Distributor 103 is fixed in tower body 101 and at tower top outlet 101b, to cause phegma (follow-up explanation) more uniformly to divide
Cloth is to filler surface.Muff 104 is sheathed on the outer wall of tower body 101, and comprising the vacuum jacket with the wall coaxial of tower body 101 and
The glass bead being filled in vacuum jacket.Wherein, glass bead is a kind of environment-friendly type novel light heat-insulating material, has matter
Gently, adiabatic, insulation, fire prevention, the features such as water absorption rate is low, the heat insulation effect of muff 104 can further be strengthened；But this implementation
Mode is not intended to be limited in any to the concrete structure and material of muff.
In addition, rectifying column 10 also adds comprising being respectively arranged at bottom of towe with two temperature display alarms, bottom of towe at tower top
The elements such as hot device (not shown), for accurately controlling the tower top of rectifying column and the temperature of bottom of towe.For example, the rectifying with FT wax products
Exemplified by, five temperature ranges for evaporating section be divided into 120 DEG C~170 DEG C, 170 DEG C~190 DEG C, 190 DEG C~210 DEG C, 210 DEG C~
280 DEG C, 280 DEG C~350 DEG C, i.e. in respectively evaporating in temperature range corresponding to section, minimum is tower top temperature, and peak is bottom of towe
Temperature.
In present embodiment, material boils module 11 and includes vapor-liquid separation tank 111, material cooling tank 112, Matter Transfer again
Pipeline 113, Matter Transfer pump 114, material heater 115 and nozzle 116.Vapor-liquid separation tank 111 is used to separate vapor-phase material
With liquid phase material and for housing liquid phase material.Specifically, the vapor-phase material outlet 111a of vapor-liquid separation tank 111 is connected to tower
The bottom of towe entrance 101a of body 101, vapor-phase material export 111a and bottom of towe entrance 101a from vapor-liquid separation tank 111 by vapor-phase material
Into in tower body 101.
Material cooling tank 112 includes tank body 1121 and heat-exchanger rig 1122.Specifically, the charging aperture connection of tank body 1121
111b is exported in the liquid phase material of vapor-liquid separation tank 111, the discharging opening of tank body 1121 is connected to the charging of Matter Transfer pipeline 113
Mouthful.
Heat-exchanger rig 1122 for example with cooling water as refrigerant, comprising heat exchanger tube 1122-1, condenser 1122-2 and
Small pump 1122-3.Heat exchanger tube 1122-1 is arranged in tank body 1121.Condenser 1122-2 is connected to heat exchanger tube 1122-1 and position
Above heat exchanger tube 1122-1.In heat transfer process, it is transformed into vapor after the cooling water heat absorption in heat exchanger tube 1122-1
And condenser 1122-2 is risen to, liquid phase water is converted into after being condensed and is back to heat exchanger tube 1122-1, so as to realize to tank body
The cycle heat exchange of liquid phase material in 1121.Small pump 1122-3 is connected to heat exchanger tube 1122-1 and thinks supplement in heat exchanger tube 1122
Cooling water.Preferably, heat-exchanger rig 1122 also includes buoyancy test section 1122-4, buoyancy test section 1122-4 is connected to heat exchanger tube
Between 1122-1 and condenser 1122-2, while it is connected to small pump 1122-3.Small pump 1122-3 can detect according to buoyancy
Portion 1122-4 controls whether to need to supplement cooling water in heat exchanger tube 1122-1 to the detection case of vapor.However, this implementation
Mode exchanges the concrete structure of thermal and the refrigerant of use is not intended to be limited in any.
The charging aperture of Matter Transfer pipeline 113 is connected to the liquid phase material outlet 111b of vapor-liquid separation tank, Matter Transfer pipe
The discharging opening on road 113 is connected to the liquid phase material import 111c of vapor-liquid separation tank by nozzle 116；Matter Transfer pump 114 and thing
Material heater 115 is respectively arranged at Matter Transfer pipeline 113, and material heater 115 compared with Matter Transfer pump 114 close to nozzle
116。
Matter Transfer pump 114 is essentially a booster pump, for the liquid phase material in Matter Transfer pipeline 113 to be pressurized
To preset pressure, the preset pressure is, for example, more than 40bar.Matter Transfer pump 114 in present embodiment is screw pump, its energy
Continuous liquid phase material under high pressure conditions is enough provided.However, present embodiment is not intended to be limited in any to this.
Material heater 115 is used to the liquid phase material under high pressure conditions being heated to preset temperature, and the preset temperature is higher than
Boiling point of the objective fraction under normal temperature.In present embodiment, material heater 115 is a kind of high efficiency heater, comprising with leading
The copper core of chute, the copper sheathing being sheathed on outside copper core and the multiple heating rods being embedded in copper core and copper sheathing.Liquid phase material passes through
During copper core guiding gutter, copper core and copper sheathing are simultaneously by heat transfer caused by multiple heating rods to liquid phase material, so as to quickly heat
The liquid phase material.However, present embodiment is not intended to be limited in any to the concrete structure of material heater, as long as can realize quick
Heat the effect of liquid phase material.
Material boils module 11 again can also include multiple electric-heating belts, be respectively arranged at vapor-liquid separation tank 111, material cooling
On tank 112, Matter Transfer pipeline 113, electric-heating belt 117 is used to play insulation effect to liquid phase material.If for example, objective fraction
Rectification temperature before cracking temperature, then maintain liquid phase substance temperature be higher than initial boiling point in initial boiling point, electric-heating belt temperature control
10-30 degree；If the rectification temperature of objective fraction after cracking temperature, maintains the temperature of liquid phase substance in cracking point, electric companion
Tropical temperature control is less than cracking point 10-30 degree；Present embodiment is not intended to be limited in any to the specific number of electric-heating belt, this area skill
Art personnel can design according to being actually needed.
In present embodiment, liquid phase material exports 111b from the liquid phase material of vapor-liquid separation tank 111 and cooled down into material
Tank 112, Matter Transfer pipeline 113 is directed to after being cooled down by material cooling tank 112.The mistake flowed in Matter Transfer pipeline 113
Journey, liquid phase material are pressurized to preset pressure (be, for example, more than 40bar) and by towards the side of nozzle 116 by Matter Transfer pump 114
To push；Liquid phase material under high pressure conditions is heated to preset temperature (higher than target distillate in normal temperature by material heater 115
Under boiling point) after, vapor-liquid separation tank 111 is spurted into by nozzle 116, now, liquid phase material atomization coexisted with forming vehicle repair major
State.When i.e., due to being injected into vapor-liquid separation tank 111, liquid phase material decompression cools simultaneously, is Partial Liquid Phase material (bag
Containing objective fraction) provide the latent heat of vaporization；That is, Partial Liquid Phase material changes into vapour phase first runnings after absorbing the latent heat of vaporization.
Because the liquid phase material under high pressure conditions is when being heated to cracking reaction temperature, heat is less likely to occur in the short time
Cracking reaction, therefore, when cracking reaction temperature is heated within by the short time, the liquid phase material still under high pressure conditions is basic
On cracking reaction does not occur.Then, when spurting into vapor-liquid separation tank 111 by nozzle 116, vapour phase is isolated from liquid phase material
First runnings.Therefore, the material that present embodiment provides boils module again can delay under reduced pressure atmosphere or even avoid liquid phase material
Cracking reaction occurs in vapor-liquid separation tank 111.Further, material cooling tank 112 be directly connected in vapor-liquid separation tank 111 with
Liquid phase material in vapor-liquid separation tank 111 is cooled down, so as to prevent liquid phase material from being split in Matter Transfer pipeline 113
Solution reaction.
In present embodiment, condensation module 12 includes shell-and-tube heat exchanger 121 and heat transferring medium EGR 122.Tool
For body, shell-and-tube heat exchanger 121 is internally divided into tube side space and shell side space.Heat transferring medium EGR 122 is connected to
Shell-and-tube heat exchanger 121 and be communicated in shell side space, the tower top outlet 101b of rectifying column 10 be connected to shell-and-tube heat exchanger 121 and
Tube side space is communicated in, to cause vapour phase first runnings to enter tube side space by the tower top outlet 101b of rectifying column 10.
Heat transferring medium EGR 122 includes medium circulation pipeline 1221, medium storage tank 1222, medium circulation pump 1223
And dielectric heater 1224.Specifically, the both ends of medium circulation pipeline 1221 be connected to shell-and-tube heat exchanger 121 and
It is communicated in shell side space.Medium storage tank 1222, medium circulation pump 1223, dielectric heater 1224 are respectively arranged at medium circulation
On pipeline 1221.Medium circulation pump 1223 is used to drive heat transferring medium in medium circulation pipeline 1221 and shell side space inner recirculation flow
It is dynamic, to cool down the vapour phase first runnings in tube side space；The heat transferring medium that dielectric heater 1224 is used in warming cycle, makes
It is constant at the temperature needed for heat exchange.Heat transferring medium is, for example, oil product, and medium storage tank 1222 is, for example, oil storage tank (comprising oiling
The parts such as mouth, oil return opening, pressure gauge, aeration valve, filter), medium circulation pump 1223 is, for example, high temperature oil pump.However, this reality
The concrete structure for applying mode heat exchanging media recycler is not intended to be limited in any.
Condensation module 12 can also include at least one electric-heating belt, be arranged on medium circulation pipeline 1221, with to following
Heat transferring medium during ring is incubated.However, present embodiment is not intended to be limited in any to this.
In heat transfer process, a part of vapour phase first runnings are condensed and change into liquid phase material in tube side space, i.e. shape
Into phegma, the phegma is back to rectifying column 10 by the tower top outlet 101b of tower body 101, and is entered by the bottom of towe of tower body 101
Mouth 101a is back to vapor-liquid separation tank 111；And the uncooled vapour phase first runnings into liquid phase are to form vapour phase to distillate in tube side space
Thing.In present embodiment, vapour phase distillate is isolated by the way of infinite reflux, is effectively improved between each fraction section
Cutting accuracy, improve fractionated products quality.
In present embodiment, material discharging module 13 include discharging pipeline 131, discharging condensing unit 132, tee pipe fitting 133,
Collecting tank 134, exhaust gas processing device 135 and blow device 136.The charging aperture 131a of discharging pipeline 131 is connected to shell-and-tube
Heat exchanger 121 and tube side space is communicated in, to receive vapour phase first runnings.Discharging condensing unit 132 be arranged at discharging pipeline 131 with
Condensation enters the vapour phase distillate of discharging pipeline 131.Specifically, discharging condensing unit 132 is included as pipeline set folder 1351, water
Circulating pump 1352, water bath with thermostatic control 1353 and water circulating pipe 1354.Pipeline set folder 1351 is sheathed on the discharging outer wall of pipeline 131,
And pass through water circulating pipe 1354 with cooling cavities and the water inlet and delivery port that are connected with cooling cavities, water bath with thermostatic control 1353
It is connected to the water inlet and delivery port of pipeline set folder 1351.Water-circulating pump 1352 is arranged at water bath with thermostatic control 1353 or is arranged at water
On circulating line 1354.Water bath with thermostatic control 1353 is used to provide temperature constant cooling water, and water-circulating pump 1352, which is used to drive, to be cooled down
Water shuttling movement between water bath with thermostatic control 1353, water circulating pipe 1354 and pipeline set folder 1351, with cooling discharging pipeline 131
Vapour phase distillate.Wherein, vapour phase distillate includes objective fraction and non-targeted fraction, after vapour phase distillate is cooled, target
Fraction changes into target distillate, and non-targeted fraction remains in that vapor phase.
, can when objective fraction has difference boiling point due to providing cooling water as heat transferring medium using water bath with thermostatic control
With by controlling the temperature of cooling water come the accurate chilling temperature for controlling vapour phase distillate.By taking the rectifying of FT wax products as an example,
When carrying out low-carbon fraction section (higher boiling) rectifying, the refrigerant from water bath with thermostatic control is chilled water (temperature is relatively low), to strengthen condensation
Effect and product yield.When proceeding to high-carbon fraction section (higher boiling hard wax and soft wax) rectifying, the refrigerant from water bath with thermostatic control
For warm water (generally more than 80 degree), while the heat exchange needs of condensation are met, can prevent higher boiling component (hard wax with
Soft wax) temperature is too low and become solid after condensation, and then causes the pipe blocking that discharges.
In present embodiment, first to the 3rd connection mouth of pipe of tee pipe fitting 133 is connected to discharging pipeline 131
Discharging opening 131b, collecting tank 134 and exhaust gas processing device 135, wherein, the first connection mouth of pipe is relative with the 3rd connection mouth of pipe
Should.After vapour phase distillate is cooled in the pipeline 131 that discharges, having been converted to the objective fraction of liquid phase state, (i.e. target distillates
Liquid) with remaining as the non-targeted fraction of vapor phase together it is connected the internal cavity that the mouth of pipe enters tee pipe fitting 133 by first；
Target distillate is dropped onto in collecting tank 134 by the 3rd connection mouth of pipe, and the non-targeted fraction of vapour phase passes through the second connection mouth of pipe
Into exhaust gas processing device 135.
Preferably, the discharging opening 131b of discharging pipeline 131 stretches into the threeway cavity of tee pipe fitting 133 from the first connection mouth of pipe
It is interior, and discharging opening 131b external diameter is less than the external diameter of the 3rd connection mouth of pipe.So as to which target distillate can be from discharging opening 131b
Directly dropped onto in collecting tank 134 via the 3rd connection mouth of pipe, avoid the wall built-up of target distillate from remaining and outside collecting tank 134
Solidification.
In addition, material discharging module 13 also includes the first connection valve 137, it is arranged on discharging pipeline 131 close to charging aperture
At 131a, for cutting off or turning on the connection between material discharging module 13 and rectifying column 10, to control whether vapour phase distillate exports
To material discharging module 13.
In addition, material discharging module 13 also includes distillate viewer (not shown), tee pipe fitting 133 is arranged at, for observing
The current drippage situation of target distillate, to judge when whether the cutting of foreshot section is completed.Wherein, distillate viewer is, for example,
Visor, shooting are first-class, and present embodiment is not restricted to this
In present embodiment, exhaust gas processing device 135 comprises at least and removes vavuum pump 1351, for exporting the non-mesh of vapour phase
Mark fraction.Preferably, exhaust gas processing device 135 can also include tail gas condenser 1352, (figure is not with non-targeted Fraction collection tank
Signal), tail gas condenser 1352 is connected to the second connection mouth of pipe of tee pipe fitting 133 and gone between vavuum pump 1351, with condensation
The non-targeted fraction of vapour phase, non-targeted Fraction collection tank are connected to after tail gas condenser 1352 is condensed with collection and change into liquid phase
Non-targeted fraction.By taking the rectifying of FT wax products as an example, when proceeding to high-carbon fraction section (higher boiling hard wax and soft wax) rectifying,
Because the temperature of the non-targeted fraction of the vapour phase of output is higher, if the non-targeted fraction of vapour phase directly by go vavuum pump 1351 (
Under normal temperature state) export, the non-targeted fraction of vapour phase may be in going in vavuum pump 1351 (being under normal temperature state) to convert
Into liquid phase, so as to which easily obstruction removes vavuum pump 1351.Therefore, tail gas condenser 1352 is carried out to the non-targeted fraction of vapour phase first
Condensation so that the higher non-targeted fraction of condensing temperature is converted into liquid in tail gas condenser 1352 and drops to non-targeted evaporate
In part collecting tank, and the relatively low non-targeted fraction of condensing temperature remains as vapour phase and is gone vavuum pump 1351 normally to export.So as to,
To some it is high boiling evaporate component and be segmented when, tail gas condenser 1352 carries out condensation process to non-targeted fraction can be to prevent
Vavuum pump 1351 is only gone to block.Wherein, tail gas condenser is, for example, shell-and-tube heat exchanger, and heat transferring medium is, for example, cooling water, and
The temperature of cooling water can be adjusted according to being actually needed.
In addition, exhaust gas processing device also includes the connection valve 1354 of check valve 1353 and second, tail gas condensing is sequentially connected to
Device 1352 and go between vavuum pump 1351 (follow-up explanation).However, present embodiment to the concrete structure of exhaust gas processing device not
Impose any restrictions, as long as the purpose of processing tail gas can be reached.
In present embodiment, blow device 136 mainly adds comprising purging source 1361, scavenging pipeline 1362 and purge gass
Hot device 1363.One end of scavenging pipeline 1362 be connected to discharging pipeline 131 and close to discharging pipeline 131 charging aperture 131a
Place, the other end are connected to purging source 1361.It is pre- to be carried out to purge gass that purging hot-air heater 1363 is arranged at scavenging pipeline 1362
Heat.
After foreshot section is cut, first, the first connection valve 137 and the second connection valve 1354 are closed, is opened simultaneously
Check valve 1353；So as to cut off the connection between discharge nozzle road 131 and rectifying column 10 and cut-out goes vavuum pump 1351 and tail gas cold
Connection between condenser 1352.Secondly, blow device 136 is opened, the purge gass after control preheating enter discharging pipeline 131, with
The target distillate of purging wall built-up makes it drop onto in collecting tank 134；Check valve 1353 of the purge gass from exhaust gas processing device 125
Middle export.Wherein, purge gass are, for example, the inert gases such as nitrogen, argon gas, helium.
It is noted that each module involved in present embodiment is logic module, and in actual applications, one
Individual logic unit can be a part for a physical location or a physical location, can also be with multiple physics lists
The combination of member is realized.In addition, in order to protrude the innovative part of the present invention, will not be with solving institute of the present invention in present embodiment
The unit that the technical problem relation of proposition is less close introduces, but this is not intended that in present embodiment and other lists are not present
Member.
It will be understood by those skilled in the art that the respective embodiments described above are to realize the specific embodiment of the present invention,
And in actual applications, can to it, various changes can be made in the form and details, without departing from the spirit and scope of the present invention.
Claims (14)
1. a kind of material boils module again, for providing vapor-phase material for rectifying column, the material boils module and included again：Vapor-liquid separation
Tank, Matter Transfer pipeline, Matter Transfer pump, material heater, liquid phase material, the material are stored in the vapor-liquid separation tank
The charging aperture of circulation line is connected to the liquid phase material outlet of the vapor-liquid separation tank, and the discharging opening of the Matter Transfer pipeline connects
The liquid phase material import of the vapor-liquid separation tank is connected to, the Matter Transfer pump and the material heater are arranged at the material
Circulation line；Also included characterized in that, the material boils module again：Nozzle；
The discharging opening of the Matter Transfer pipeline is connected to the liquid phase material import of the vapor-liquid separation tank by the nozzle；
The Matter Transfer pump is used to be pressurized the liquid phase material, and the material heater is used for the liquid phase material
Heated, the material heater Matter Transfer pump is close to the nozzle；
The liquid phase material is spurted into the vapor-liquid separation tank by the nozzle, to cause the liquid phase material of part to change into
The vapor-phase material.
2. material according to claim 1 boils module again, it is characterised in that the Matter Transfer pump is screw pump.
3. material according to claim 1 boils module again, it is characterised in that it is also cold comprising material that the material boils module again
But tank, it is connected between the liquid phase material outlet of the vapor-liquid separation tank and the charging aperture of the Matter Transfer pipeline, the thing
Material cooling tank is directed to the Matter Transfer pipeline after the liquid phase material is cooled down.
4. material according to claim 3 boils module again, it is characterised in that the material cooling tank includes tank body and heat exchange
Device, the heat-exchanger rig are arranged at the tank body, and the heat-exchanger rig is used to cool down the liquid phase material in the tank body.
5. material according to claim 1 boils module again, it is characterised in that the material boils module and also includes multiple electricity again
Heating tape, it is respectively arranged at the vapor-liquid separation tank and the Matter Transfer pipeline.
6. a kind of distillation system, it is characterised in that include：
The material described in any one in claim 1 to 5 boils module again；
Rectifying column, the bottom of towe entrance of the rectifying column are connected to the material and boil module again, and the rectifying column is used for from the vapour
Vapour phase first runnings are isolated in phase materials, objective fraction is included in the vapour phase first runnings；
Condensation module, is connected to the tower top outlet of the rectifying column, the condensation module be used to condensing the vapour phase first runnings with
Vapour phase distillate is isolated from the vapour phase first runnings, the objective fraction is included in the vapour phase distillate；
Material discharging module, is connected to the condensation module, and the material discharging module is described to cause for condensing the vapour phase distillate
Objective fraction is converted into target distillate.
7. distillation system according to claim 6, it is characterised in that the condensation module includes shell-and-tube heat exchanger with changing
Thermal medium EGR, the heat transferring medium EGR are connected to the shell-and-tube heat exchanger and are communicated in the shell-and-tube and change
The shell side space of hot device, the rectifying column are connected to the shell-and-tube heat exchanger and are communicated in the tube side of the shell-and-tube heat exchanger
Space.
8. distillation system according to claim 7, it is characterised in that the heat transferring medium EGR includes medium circulation
Pipeline, medium circulation pump and dielectric heater, the both ends of the medium circulation pipeline are connected to the pipe shell type heat exchange
Device and the shell side space is communicated in, the medium circulation pump is respectively arranged at the medium circulation pipe with the dielectric heater
Road, the medium circulation pump driving heat transferring medium circulate between the shell side space and the medium circulation pipeline, with
Cool down the vapour phase first runnings in the tube side space.
9. distillation system according to claim 6, it is characterised in that the material discharging module is cold comprising discharging pipeline, discharging
Solidifying device and collecting tank, the charging aperture of the discharging pipeline are connected to the condensation module and the collection with discharging opening
Tank, the discharging condensing unit are arranged at the discharging pipeline to cool down the vapour phase distillate in the discharging pipeline so that institute
Objective fraction is stated to change into the target distillate and enter the collecting tank.
10. distillation system according to claim 9, it is characterised in that the material discharging module also includes tee pipe fitting and tail
Flash Gas Compression Skid System, the tee pipe fitting are connected to discharging opening, the collecting tank and the vent gas treatment of the discharging pipeline
Device.
11. distillation system according to claim 10, it is characterised in that the material discharging module also includes blow device, even
It is connected to the discharging pipeline and is attached to the discharging for purging close to the charging aperture of the discharging pipeline, the blow device
Target distillate on pipeline inner wall.
12. distillation system according to claim 10, it is characterised in that the material discharging module is also observed comprising distillate
Device, it is arranged at the tee pipe fitting.
13. distillation system according to claim 9, it is characterised in that the discharging condensing unit includes pipeline set folder, water
Circulating pump and water bath with thermostatic control, the pipeline set chuck are located at the discharging pipeline, and the water bath with thermostatic control is connected to the pipeline
The water inlet and delivery port of folder are covered, the water-circulating pump is arranged at the water bath with thermostatic control, and the water-circulating pump, which is used to drive, to be cooled down
Water circulates between the water bath with thermostatic control and pipeline set folder, to cool down the vapour phase distillate in the discharging pipeline.
14. distillation system according to claim 6, it is characterised in that the rectifying column includes tower body and muff, described
Muff is sheathed on the tower body outer wall.
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| CN201410855678.8A CN105797415B (en) | 2014-12-31 | 2014-12-31 | A kind of material boils module and applies its distillation system again |
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| CN201410855678.8A CN105797415B (en) | 2014-12-31 | 2014-12-31 | A kind of material boils module and applies its distillation system again |
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| CN105797415A CN105797415A (en) | 2016-07-27 |
| CN105797415B true CN105797415B (en) | 2018-03-30 |
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| CN110694291B (en) * | 2019-10-31 | 2021-09-10 | 周孝威 | Pressure reducing device with early warning for distillation tower |
| CN114733221B (en) * | 2022-04-24 | 2023-03-28 | 南通利奥化工科技有限公司 | Rectifying tower for quickly heating and vaporizing materials |
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| US7837768B2 (en) * | 2007-08-27 | 2010-11-23 | General Electric Capital Corporation As Administrative Agent | System and method for purifying an aqueous stream |
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| WO2011041732A2 (en) * | 2009-10-01 | 2011-04-07 | Mississippi State University | Method to upgrade bio-oils to fuel and bio-crude |
| CN102309865A (en) * | 2011-09-08 | 2012-01-11 | 中国石油天然气集团公司 | Refining system for circulating 1, 3-propanediol in continuous production of poly(trimethylene terephthalate) |
| JP5954530B2 (en) * | 2012-03-30 | 2016-07-20 | 栗田工業株式会社 | Sulfuric acid waste liquid treatment apparatus and sulfuric acid waste liquid treatment method |
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| CN105797415A (en) | 2016-07-27 |
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