CN105964005B - A kind of partition type MVR heat pump distillations are thermally integrated system - Google Patents
A kind of partition type MVR heat pump distillations are thermally integrated system Download PDFInfo
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- CN105964005B CN105964005B CN201610256631.9A CN201610256631A CN105964005B CN 105964005 B CN105964005 B CN 105964005B CN 201610256631 A CN201610256631 A CN 201610256631A CN 105964005 B CN105964005 B CN 105964005B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/324—Tray constructions
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of partition type MVR heat pump distillations to be thermally integrated system, and the system comprises feeding preheating part, cyclic part, upper tower rectifying part, compression condensation part, water emitting portion, lower tower rectifying part, vapor heating part, product discharge part, condensed water discharge part, kettle liquid discharge part, cooling segment.The present invention can be used in some special big temperature difference separation processes, the system directly compresses the gas being ejected from upper tower rectifying tower, improve the pressure and condensation temperature of overhead gas, heat source as the upper tower reboiler of upper tower rectifying column, take full advantage of by the condensation latent heat of compressed gas, while reduce the consumption of the hot public work of tower reactor and the cold public work of tower top.For relatively traditional rectifying, more economical, energy saving using the form, investment cost is moderate, and control is simple, only need to consume the vapor of a small amount of lowest level, while saves the vapor of a large amount of greater degrees, which can produce huge economic benefit.
Description
Technical field
The present invention relates to a kind of energy-efficient technology in industrial rectifying field, using directly compressing overhead gas,
And main distillation column is divided into the mode of upper and lower two tower, it is applied to big temperature difference separation process, to reduce the consumption of vapor
And carry out energy saving.
Background technology
At present, industrial distillation operation uses multi-effect distillation, and due to the increase with effect number, heating steam consumption reduces what is produced
Energy-saving effect starts constantly to decline, and is limited by first order heating steam pressure and final stage cooling medium species, and operation is more
Difficulty, while the factor such as property also by separation mixture, volatile components content, technological process is influenced；Its related energy saving base
Originally the limit is had reached, continuous with yield expands, its energy consumption is very huge.
Domestic and foreign scholars have done in the rectifying effect number of rectifying, charge order, feed entrance point, heat-exchange network etc. and have largely ground
Study carefully, it is proposed that many prioritization schemes, have reached certain energy-saving effect.But multi-effect distillation still suffers from some shortcomings：
(1) multi-effect distillation is by setting the different rectifying column of some operating pressures, the steam of each column overhead of cascade utilization, but
It is that the minimum rectifying column tower top steam of operating pressure is still needed with a large amount of circulating waters, at the same time must consumes a large amount of
Vapor carrys out the highest tower bottom of rectifying tower liquid of heating operation pressure, causes the dual consumption of hot and cold public work；
(2) operation temperature of each tower tower reactor is raised with the rise of operating pressure, it is necessary to a variety of pressure in multi-effect distillation
The fresh water steam of grade is as heat source；
(3) nominal increase rectifying effect number can be more energy saving, but this is limited by full factory's water vapor levels, and with
Operating pressure improves, and the relative volatility of material diminishes, required reflux ratio bigger, and the energy-saving effect of increase rectifying effect number becomes not
Substantially.
CN103285615B and CN103566612B discloses a kind of conventional formula heat pump rectification system.From Technological Economy angle
Degree considers that conventional heat pump rectifying is usually only applicable to bottom of towe and the less occasion of the tower top temperature difference, and the temperature difference is smaller, required compression
Work(is smaller, and the performance of heat pump is better.For some special big temperature difference separation processes (such as methanol, DMAC rectifying), using point
Cut that formula heat pump distillation flow is more economical, this flow takes tower installation heat pump and lower tower to reduce the energy conservation measure of regurgitant volume,
Energy-saving effect is obvious, and investment cost is moderate, and control is simple.
The content of the invention
The technical problems to be solved by the invention are：Overcome the shortcomings of the prior art, propose a kind of more efficient section
The partition type MVR heat pump distillations of energy are thermally integrated system.
In order to solve the above-mentioned technical problem, the technical scheme is that：A kind of partition type MVR heat pump distillations, which are thermally integrated, is
System, the system comprises feeding preheating part, upper tower rectifying part, cyclic part, compression condensation part, water emitting portion, lower tower
Rectifying part, vapor heating part, product discharge part, condensed water discharge part, kettle liquid discharge part, cooling segment；
The feeding preheating part is connected with upper tower rectifying part, and upper tower rectifying part is connected with cyclic part, pressure
Contracting condensation portion is connected with upper tower rectifying part, and water emitting portion is connected with compression condensation part, lower tower rectifying part with it is upper
Tower rectifying part is connected, and vapor heating part is connected with upper tower rectifying part, lower tower rectifying part respectively, product discharge
Part be connected respectively with feeding preheating part, compression condensation part, condensed water discharge part respectively with upper tower rectifying part, under
Tower rectifying part, feeding preheating part are connected, and kettle liquid discharge part is connected with lower tower rectifying part, feeding preheating part respectively
Connect, cooling segment is connected with compression condensation part.
Further, the feeding preheating part includes sequentially connected feed supplement pump (P01), feed storage tank (R01), feed pump
(P02), upper tower feed flow meter (FI01), level-one preheater (E01), two level preheater (E02), three-level preheater (E03), on
Tower rectifying column (T01), lower tower rectifying column (T02)；The feeding preheating part is pre- by material liquid by one, two, three preheater
Heat arrives bubble point, feeds supreme tower rectifying column (T01) and carries out normal rectifying separation, and feeds to lower tower rectifying column (T02) and be served only for
Feed supplement when system is initially driven, supreme tower rectifying column (T01) is fed by valve (V01) control, by valve (V02) control charging extremely
Lower tower rectifying column (T02).
Further, the upper tower rectifying part includes sequentially connected upper tower rectifying column (T01) and concurrent heating separation chamber
(E05)；The upper tower rectifying column (T01) is plate column rectifying separation equipment or packed tower rectifying separation equipment or hypergravity rectifying
Machine；The concurrent heating separation chamber (E05) is the overall separation chamber with concurrent heating function or the separated separation with outer heating device
Room.
Further, the cyclic part includes sequentially connected concurrent heating separation chamber (E05), upper tower circulating pump (P04), upper tower
Reboiler (E06)；The upper tower reboiler (E06) is shell and tube reboiler or spiral plate type reboiler or board-like reboiler or spiral shell
Revolve wound form reboiler.
Further, the compression condensation part includes sequentially connected upper tower rectifying column (T01), compressor (C01), saturation
Device (R02), upper tower reboiler (E06), product surge tank (R03)；The compressor (C01) is centrifugal compressor or roots-type
Compressor or screw compressor；Saturator (R02) bottom is equipped with a water seal arrangement, and the unnecessary water spray of system is through water seal
Product surge tank (R03) is flowed into after device.
Further, the water emitting portion includes sequentially connected product surge tank (R03), upper tower discharge pump (P06), water spray
Flowmeter (FI03), saturator (R02), product surge tank (R03).
Further, the lower tower rectifying part includes sequentially connected lower tower feed pump (P05), lower tower feed flow meter
(FI02), lower tower rectifying column (T02), lower tower reboiler (E04)；After the lower tower feed pump (P05) by valve (V05) control into
Material is back to upper tower rectifying column (T01) to lower tower rectifying column (T02) by valve (V06) control；The lower tower rectifying column (T02)
Natural Circulation is carried out with lower tower reboiler (E04) to separate.
Further, the vapor heating part includes sequentially connected raw vapour source, lower tower reboiler (E04), concurrent heating
Separation chamber (E05).
Further, the product discharge part include sequentially connected upper tower discharge pump (P06), level-one preheater (E01),
Finished product flowmeter (FI05), finished product storage tank (R04), finished product unloading pump (P07) and return flow meter (FI04), upper tower rectifying column
(T01)；The finished product flowmeter (FI05) is adjusted by valve (V11), and the return flow meter (FI04) passes through valve (V10)
It is adjusted.
Further, the condensed water discharge part includes sequentially connected condensate pump (P08), condensation flow gauge
(FI06), two level preheater (E02).
Further, the kettle liquid discharge part includes sequentially connected lower tower reactor liquid pump (P03), kettle liquid flowmeter
(FI07), three-level preheater (E03), kettle liquid storage tank (R05)；The kettle liquid flowmeter (FI07) is adjusted by valve (V04).
Further, the cooling segment includes sequentially connected product surge tank (R03), gas condenser (E07), charging
Storage tank (R01), and cooling water storage tank (R06), cooling water pump (P10), cooling water flow meter (FI08)；The gas condenser
(E07) condensate outlet pipeline needs to form fluid-tight in fully-inserted feed storage tank (R01).
After employing above-mentioned technical proposal, the invention has the advantages that：
(1) system is more energy-efficient than other systems more science, has that operating cost is low, easy to adjust, work
The advantages that stablizing；
(2) system can be full recycled to receipts using such as methanol, ethanol, isopropanol, DMAC, DMF, DMSO some spies
Indirect steam in different big temperature difference separation process and achieve the purpose that energy saving；
(3) system directly compresses the gas that tower top comes out, and takes full advantage of by the condensation latent heat of compressed gas, subtracts at the same time
The small consumption of the hot public work of tower reactor and the cold public work of tower top；
(4) consider that more economical using separated heat pump distillation flow, this flow takes tower from Technological Economy angle
Heat pump is installed and lower tower reduces the energy conservation measure of regurgitant volume, energy-saving effect is obvious, and investment cost is moderate, and control is simple；
(5) for relatively traditional rectifying, more economical, energy saving using the form, investment cost is moderate, and control is simple, only
The vapor (such as 0.3MPa) of a small amount of lowest level need to be consumed, while saves the vapor (such as 1.0MPa) of a large amount of greater degrees,
Huge economic benefit can be produced.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
There is attached drawing needed in technology description to be briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, without creative efforts, can be with
Other attached drawings are obtained according to these attached drawings.
Fig. 1 is that a kind of partition type MVR heat pump distillations of the present invention are thermally integrated the process flow chart of system；
Fig. 2 is the process flow chart of single tower distillation；
Fig. 3 is the process flow chart of double-effect rectification；
Fig. 4 is the process flow chart of single column heat pump distillation；
Code name represents as follows respectively in figure：
Feed supplement pump (P01), feed pump (P02), lower tower reactor liquid pump (P03), upper tower circulating pump (P04), lower tower feed pump
(P05), upper tower discharge pump (P06), finished product unloading pump (P07), condensate pump (P08), kettle liquid unloading pump (P09), cooling water pump
(P10)；Level-one preheater (E01), two level preheater (E02), three-level preheater (E03), lower tower reboiler (E04), concurrent heating point
From room (E05), upper tower reboiler (E06), gas condenser (E07)；Feed storage tank (R01), saturator (R02), finished product buffering
Tank (R03), finished product storage tank (R04), kettle liquid storage tank (R05), cooling water storage tank (R06)；Upper tower feed flow meter (FI01), lower tower
Feed flow meter (FI02), water jet gauge (FI03), return flow meter (FI04), finished product flowmeter (FI05), condensation flow
Gauge (FI06), kettle liquid flowmeter (FI07), cooling water flow meter (FI08)；Upper tower rectifying column (T01), lower tower rectifying column
(T02)；Compressor (C01)；Valve (V01), valve (V02), valve (V03), valve (V04), valve (V05), valve (V06), valve (V07), valve
(V08), valve (V09), valve (V10), valve (V11).
Embodiment
In order that the present invention can be more clearly and readily understood, it is right below according to specific embodiment and with reference to attached drawing
The present invention is described in further detail.
As shown in Figure 1, a kind of partition type MVR heat pump distillations are thermally integrated system, the system comprises feeding preheating part, on
Tower rectifying part, cyclic part, compression condensation part, water emitting portion, lower tower rectifying part, vapor heating part, product row
Go out part, condensed water discharge part, kettle liquid discharge part, cooling segment；
The feeding preheating part is connected with upper tower rectifying part, and upper tower rectifying part is connected with cyclic part, pressure
Contracting condensation portion is connected with upper tower rectifying part, and water emitting portion is connected with compression condensation part, lower tower rectifying part with it is upper
Tower rectifying part is connected, and vapor heating part is connected with upper tower rectifying part, lower tower rectifying part respectively, product discharge
Part be connected respectively with feeding preheating part, compression condensation part, condensed water discharge part respectively with upper tower rectifying part, under
Tower rectifying part, feeding preheating part are connected, and kettle liquid discharge part is connected with lower tower rectifying part, feeding preheating part respectively
Connect, cooling segment is connected with compression condensation part.
Preferably, as shown in Figure 1, the feeding preheating part includes sequentially connected feed supplement pump (P01), feed storage tank
(R01), feed pump (P02), upper tower feed flow meter (FI01), level-one preheater (E01), two level preheater (E02), three-level are pre-
Hot device (E03), upper tower rectifying column (T01), lower tower rectifying column (T02)；The feeding preheating part is preheated by one, two, three
Material liquid is preheating to bubble point by device, is fed supreme tower rectifying column (T01) and is carried out normal rectifying separation, and is fed to lower tower rectifying column
(T02) feed supplement when system is initially driven is served only for, supreme tower rectifying column (T01) is fed by valve (V01) control, passes through valve
(V02) control is fed to lower tower rectifying column (T02).
Preferably, as shown in Figure 1, the upper tower rectifying part includes sequentially connected upper tower rectifying column (T01) and concurrent heating
Separation chamber (E05)；The upper tower rectifying column (T01) is plate column rectifying separation equipment, naturally it is also possible to for packed tower rectifying point
From the rectifying separation equipment of the form such as equipment or hypergravity rectifier；The concurrent heating separation chamber (E05) carries concurrent heating for overall
The separation chamber of function, can also be the separated separation chamber with outer heating device.
Preferably, as shown in Figure 1, the cyclic part includes sequentially connected concurrent heating separation chamber (E05), upper tower circulating pump
(P04), upper tower reboiler (E06)；The upper tower reboiler (E06) is shell and tube reboiler, naturally it is also possible to is spiral plate type
The reboiler of reboiler or the form such as board-like reboiler or spiral winded type reboiler.
Preferably, as shown in Figure 1, the compression condensation part includes sequentially connected upper tower rectifying column (T01), compressor
(C01), saturator (R02), upper tower reboiler (E06), product surge tank (R03)；The compressor (C01) is centrifugal compressor
Machine, can also be Roots Compressor or screw compressor certainly；Saturator (R02) bottom is equipped with a water seal and fills
Put, the unnecessary water spray of system flows into product surge tank (R03) after water seal arrangement.
Preferably, as shown in Figure 1, the water emitting portion includes sequentially connected product surge tank (R03), upper tower discharge pump
(P06), water jet gauge (FI03), saturator (R02), product surge tank (R03)；The water emitting portion is mainly used for overheat and steams
Vapour eliminates the degree of superheat.
Preferably, as shown in Figure 1, the lower tower rectifying part include sequentially connected lower tower feed pump (P05), lower tower into
Stream gauge (FI02), lower tower rectifying column (T02), lower tower reboiler (E04)；Pass through valve after the lower tower feed pump (P05)
(V05) control charging is back to upper tower rectifying column (T01), the valve to lower tower rectifying column (T02) by valve (V06) control
(V06) it is served only for flowing back when system is initially driven；The lower tower rectifying column (T02) carries out nature with lower tower reboiler (E04) and follows
Ring separates.
Preferably, as shown in Figure 1, the vapor heating part includes sequentially connected raw vapour source, lower tower reboiler
(E04), concurrent heating separation chamber (E05)；Be mainly used for heating lower tower reboiler (E04) and to concurrent heating separation chamber (E05) into
Row concurrent heating.
Preferably, as shown in Figure 1, the product discharge part is pre- including sequentially connected upper tower discharge pump (P06), level-one
Hot device (E01), finished product flowmeter (FI05), finished product storage tank (R04), finished product unloading pump (P07) and return flow meter (FI04),
Upper tower rectifying column (T01)；The finished product flowmeter (FI05) is adjusted by valve (V11), the return flow meter (FI04)
It is adjusted by valve (V10).
Preferably, as shown in Figure 1, the condensed water discharge part includes sequentially connected condensate pump (P08), condensed water
Flowmeter (FI06), two level preheater (E02).
Preferably, as shown in Figure 1, the kettle liquid discharge part includes sequentially connected lower tower reactor liquid pump (P03), kettle liquid stream
Gauge (FI07), three-level preheater (E03), kettle liquid storage tank (R05)；The kettle liquid flowmeter (FI07) is carried out by valve (V04)
Adjust, the valve (V03) is served only for using when feeding concurrent heating separation chamber (E05) when system is initially driven.
Preferably, as shown in Figure 1, the cooling segment includes sequentially connected product surge tank (R03), gas condenser
(E07), feed storage tank (R01), and cooling water storage tank (R06), cooling water pump (P10), cooling water flow meter (FI08)；It is described
Gas condenser (E07) condensate outlet pipeline needs to form fluid-tight in fully-inserted feed storage tank (R01).
The operation principle of the present invention is as follows：
The main distillation column of separated heat pump distillation flow is divided into two towers up and down：Upper tower is similar to conventional heat pump rectifying, simply
More feed inlets；And lower tower is similar to the stripping section of conventional rectification, the kettle liquid from upper tower is fed, steam discharging then enters
Upper tower bottom of towe.Can be by controlling cut-point concentration (descending tower input concentration) to make upper tower temperature difference smaller, so as to reduce compressor
Required compression ratio, reduces investment and operating cost, shortens the payoff period of additional investment.Upper tower installation heat pump can obtain preferable effect
Fruit, heat pump heat supply coefficient COP are larger；Meanwhile the regurgitant volume of lower tower can also greatly reduce, vapor consumption is reduced.
Preferably, the feed supplement pump (P01) of the system carries out feed supplement to feed storage tank (R01), and feed pump (P02) is from charging
Storage tank (R01) charging is pre- by level-one using the product of discharge after upper tower feed flow meter (FI01) carries out flow control
Hot device (E01) to material liquid carry out level-one preheating after, using discharge condensed water by two level preheater (E02) to material liquid into
After the preheating of row two level, after carrying out three-level preheating to material liquid by three-level preheater (E03) using the kettle liquid of discharge, reach bubble point
Temperature and be directly entered tower rectifying column (T01) carry out rectifying section purification operations.
The material liquid for entering upper tower rectifying column (T01) be uniformly distributed inside it after along tower with liquid phase state from upper
Flow to tower bottom under and, and the liquid of upper tower rectifying column (T01) bottom by lower tower feed pump (P05) to lower tower rectifying column
(T02) fed, equally flow to tower bottom along tower with liquid phase state is top-down, and the liquid of lower tower rectifying column (T02) bottom
Body carries out Natural Circulation evaporation with lower tower reboiler (E04) by lower tower rectifying column (T02) and separates, and using raw steam to lower tower
Reboiler (E04) is heated, and after tower bottoms reaches the concentration of emission request, discharge is carried out by lower tower reactor liquid pump (P03),
Flow control is carried out using kettle liquid flowmeter (FI07), it is pre- to carry out three-level to material liquid subsequently into three-level preheater (E03)
Heat, and be collected in kettle liquid storage tank (R05), shifted after filling liquid using kettle liquid unloading pump (P09).
The raw steam upper tower rectifying column (T01) is heated with lower tower reboiler (E04) after condensate liquid pass through it is cold
Condensate pump (P08) carries out discharge opeing, flow control is carried out using condensation flow gauge (FI06), subsequently into two level preheater
(E02) after carrying out two level preheating to material liquid, outer row is carried out.
Preferably, the lower tower rectifying column (T02) of the system separates with the progress Natural Circulation evaporation of lower tower reboiler (E04)
Obtained from saturated gas then along tower with gas phase state from bottom to top flow to top of tower, and with top-down liquid phase state into promoting the circulation of qi
Liquid mass transfer separates, and is finally reached gas-liquid phase equilibrium process；From lower tower rectifying column (T02) top of tower come out after saturated gas enter
Behind concurrent heating separation chamber (E05), with the saturated gas one separated from concurrent heating separation chamber (E05) and upper tower reboiler (E06)
Rise along upper tower rectifying column (T01) and flowed out with the slave top of tower of gas phase state from bottom to top, equally carried out with top-down liquid phase state
Gas-liquid mass transfer separates, and is finally reached gas-liquid phase equilibrium process.
The saturated gas from the outflow of upper tower rectifying column (T01) top of tower is compressed acting into compressor (C01)
Afterwards, the pressure and temperature of overhead gas is improved, and becomes superheated steam, and the elimination degree of superheat is carried out into saturator (R02), and
Become saturated vapor, subsequently enter in tower reboiler (E06) and carry out heat transfer condensation, after becoming liquid, be collected in finished product buffering
In tank (R03), shunted by upper tower discharge pump (P06)；A part of liquid carries out flow by finished product flowmeter (FI05)
After control, the elimination degree of superheat is carried out to the superheated steam from compressor (C01) out into saturator (R02)；Another portion
After liquid separation body then enters level-one preheater (E01) to material liquid progress level-one preheating, shunted again, a part of liquid passes through
Return flow meter (FI04) carry out flow control after, be back to tower rectifying column (T01) carry out gas-liquid mass transfer separation process, with into
One step improves product purity, and after another part liquid then carries out flow control by finished product flowmeter (FI05), it is collected in into
In product storage tank (R04), shifted after filling liquid using finished product unloading pump (P07).
The unnecessary hydrojet entered in saturator (R02), after being collected in saturator (R02) bottom, by setting fluid-tight
And it is back to product surge tank (R03).
Liquid in the concurrent heating separation chamber (E05) by tower reboiler (E06) in upper tower circulating pump (P04) entrance into
Row is heated after evaporation, is flashed and isolated product saturated gas into concurrent heating separation chamber (E05), this process is pressure
Cyclic process.
Preferably, the saturated gas or incoagulable gas not being condensed in the ready system products surge tank (R03) into
Enter after being condensed in gas condenser (E07), into feed storage tank (R01), gas condenser (E07) condensate liquid goes out
Mouth pipeline needs to form fluid-tight in fully-inserted feed storage tank (R01).The cooling water enters cooling water storage tank (R06), then
It is right into gas condenser (E07) after carrying out flow control by cooling water flow meter (FI08) into cooling water pump (P10)
The saturated gas or incoagulable gas not being condensed are cooled down, and are then discharged.
In actual production, exemplified by producing 600000 tons of methanol per year, using partition type MVR heat pump distillations heat collection as shown in Figure 1
Into the process flow chart of system.When feed conditions be 61.8 ten thousand tons, every year by 8000 it is small when produced when, feeding temperature is
71.6 DEG C, feed rate 94277kg/h, feed pressure 1.7MPaG, feed composition is methanol 82%, water 18%；Tower top will
Ask as methanol 96.8%, water 3.2%；Tower reactor requirement is methanol 0.1%, water 99.9%；Plate pressure drop is 0.7kPa in tower.
Comparative example：
Equally exemplified by producing 600000 tons of methanol per year, using process flow chart as shown in Figure 2, Figure 3, Figure 4, but other operations
Parameter all same.
For embodiment compared with comparative example, energy consumption and cost parameter contrast table are as shown in table 1, and steam and electricity consumption are all converted to
Mark coal, total conversion mark coal be compared, double-effect rectification relative to single tower distillation energy saving 18.9%, single column heat pump distillation relative to
Single tower distillation energy saving 76.48%, for separated heat pump distillation relative to single tower distillation energy saving 75.28%, single column heat pump distillation is opposite
In double-effect rectification energy saving 70.98%, separated heat pump distillation is relative to double-effect rectification energy saving 69.49%.By steam price according to
Electricity price lattice, are carried out being converted to total price being compared, double-effect rectification is opposite by 120 yuan/ton of market price according to 0.8 yuan of market price/degree
In single tower distillation cost-effective 18.98%, single column heat pump distillation is relative to single tower distillation cost-effective -38.49%, partition type warm
Rectifying is pumped relative to single tower distillation cost-effective 46.99%, single column heat pump distillation relative to double-effect rectification it is cost-effective-
70.93%, separated heat pump distillation is relative to double-effect rectification cost-effective 34.57%.
1 energy consumption of table and cost parameter contrast table
By embodiment compared with comparative example, for current industrial distillation technology, using segmentation as shown in Figure 1
When formula MVR heat pump distillations are thermally integrated the process flow chart of system than using process flow chart as shown in Figure 2, Figure 3, Figure 4, more
Economical and energy saving, production cost are lower.
The system is more energy-efficient than other systems more science, has that operating cost is low, easy to adjust, work is steady
The advantages that determining；
The system can be full recycled to receipts, and using such as methanol, ethanol, isopropanol, DMAC, DMF, DMSO, some are special
Big temperature difference separation process in indirect steam and achieve the purpose that energy saving；
The system directly compresses the gas that tower top comes out, and takes full advantage of by the condensation latent heat of compressed gas, reduces at the same time
The consumption of the hot public work of tower reactor and the cold public work of tower top；
Consider that more economical using separated heat pump distillation flow, this flow takes Shang Taan from Technological Economy angle
Fill heat pump and lower tower reduces the energy conservation measure of regurgitant volume, energy-saving effect is obvious, and investment cost is moderate, and control is simple；
For relatively traditional rectifying, more economical, energy saving using the form, investment cost is moderate, and control is simple, need to only disappear
The vapor (such as 0.3MPa) of a small amount of lowest level is consumed, while saves the vapor (such as 1.0MPa) of a large amount of greater degrees, can
Produce huge economic benefit.
Particular embodiments described above, pair present invention solves the technical problem that, technical solution and beneficial effect carry out
It is further described, it should be understood that the foregoing is merely the specific embodiment of the present invention, is not limited to this
Invention, within the spirit and principles of the invention, any modification, equivalent substitution, improvement and etc. done, should be included in this hair
Within bright protection domain.
Claims (10)
1. a kind of partition type MVR heat pump distillations are thermally integrated system, it is characterised in that the system comprises feeding preheating part, on
Tower rectifying part, cyclic part, compression condensation part, water emitting portion, lower tower rectifying part, vapor heating part, product row
Go out part, condensed water discharge part, kettle liquid discharge part, cooling segment；
The feeding preheating part is connected with upper tower rectifying part, and upper tower rectifying part is connected with cyclic part, and compression is cold
Solidifying part is connected with upper tower rectifying part, and water emitting portion is connected with compression condensation part, lower tower rectifying part and upper tower essence
Evaporate part to be connected, vapor heating part is connected with upper tower rectifying part, lower tower rectifying part respectively, product discharge part
It is connected respectively with feeding preheating part, compression condensation part, condensed water discharge part is smart with upper tower rectifying part, lower tower respectively
Evaporate part, feeding preheating part be connected, kettle liquid discharge part is connected with lower tower rectifying part, feeding preheating part respectively,
Cooling segment is connected with compression condensation part；
The compression condensation part include sequentially connected upper tower rectifying column (T01), compressor (C01), saturator (R02), on
Tower reboiler (E06), product surge tank (R03)；The compressor (C01) is centrifugal compressor or Roots Compressor or spiral shell
Rod-type compressor；Saturator (R02) bottom is equipped with a water seal arrangement, and the unnecessary water spray of system flows into after water seal arrangement
To product surge tank (R03)；
The water emitting portion includes sequentially connected product surge tank (R03), upper tower discharge pump (P06), water jet gauge
(FI03), saturator (R02), product surge tank (R03).
2. a kind of partition type MVR heat pump distillations according to claim 1 are thermally integrated system, it is characterised in that the charging
Regenerator section includes sequentially connected feed supplement pump (P01), feed storage tank (R01), feed pump (P02), upper tower feed flow meter
(FI01), level-one preheater (E01), two level preheater (E02), three-level preheater (E03), upper tower rectifying column (T01), lower tower essence
Evaporate tower (T02)；Material liquid is preheating to bubble point by the feeding preheating part by one, two, three preheater, feeds supreme tower essence
Evaporate tower (T01) and carry out normal rectifying separation, and supreme tower rectifying column (T01) is fed by valve control, by valve control charging extremely
Lower tower rectifying column (T02).
3. a kind of partition type MVR heat pump distillations according to claim 2 are thermally integrated system, it is characterised in that the upper tower
Rectifying part includes sequentially connected upper tower rectifying column (T01) and concurrent heating separation chamber (E05)；The upper tower rectifying column (T01) is
Plate column rectifying separation equipment or packed tower rectifying separation equipment or hypergravity rectifier；The concurrent heating separation chamber (E05) is whole
The separation chamber with concurrent heating function or the separated separation chamber with outer heating device of body.
4. a kind of partition type MVR heat pump distillations according to claim 3 are thermally integrated system, it is characterised in that the circulation
Part includes sequentially connected concurrent heating separation chamber (E05), upper tower circulating pump (P04), upper tower reboiler (E06)；The upper tower is again
It is shell and tube reboiler or spiral plate type reboiler or board-like reboiler or spiral winded type reboiler to boil device (E06).
5. a kind of partition type MVR heat pump distillations according to claim 4 are thermally integrated system, it is characterised in that the lower tower
Rectifying part include sequentially connected lower tower feed pump (P05), lower tower feed flow meter (FI02), lower tower rectifying column (T02), under
Tower reboiler (E04)；Controlled after the lower tower feed pump (P05) by valve control charging to lower tower rectifying column (T02) by valve
It is back to tower rectifying column (T01)；The lower tower rectifying column (T02) carries out Natural Circulation with lower tower reboiler (E04) and separates.
6. a kind of partition type MVR heat pump distillations according to claim 5 are thermally integrated system, it is characterised in that the water steams
Gas heating part includes sequentially connected raw vapour source, lower tower reboiler (E04), concurrent heating separation chamber (E05).
7. a kind of partition type MVR heat pump distillations according to claim 6 are thermally integrated system, it is characterised in that the product
Discharge part includes sequentially connected upper tower discharge pump (P06), level-one preheater (E01), finished product flowmeter (FI05), finished product storage
Tank (R04), finished product unloading pump (P07) and return flow meter (FI04), upper tower rectifying column (T01)；The finished product flowmeter
(FI05) it is adjusted by valve, the return flow meter (FI04) is adjusted by valve.
8. a kind of partition type MVR heat pump distillations according to claim 7 are thermally integrated system, it is characterised in that the condensation
Water discharge part includes sequentially connected condensate pump (P08), condensation flow gauge (FI06), two level preheater (E02).
9. a kind of partition type MVR heat pump distillations according to claim 8 are thermally integrated system, it is characterised in that the kettle liquid
Discharge part includes sequentially connected lower tower reactor liquid pump (P03), kettle liquid flowmeter (FI07), three-level preheater (E03), kettle liquid storage
Tank (R05)；The kettle liquid flowmeter (FI07) is adjusted by valve.
10. a kind of partition type MVR heat pump distillations according to claim 9 are thermally integrated system, it is characterised in that the cooling
Part includes sequentially connected product surge tank (R03), gas condenser (E07), feed storage tank (R01), and cooling water storage
Tank (R06), cooling water pump (P10), cooling water flow meter (FI08)；Gas condenser (E07) the condensate outlet pipeline needs
Want to form fluid-tight in fully-inserted feed storage tank (R01).
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| CN107583300B (en) * | 2017-10-16 | 2019-09-17 | 中国科学院理化技术研究所 | Hypergravity MVR heat pump rectification system |
| CN108079610B (en) * | 2018-01-15 | 2024-02-23 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying device and rectifying method thereof |
| CN109879722A (en) * | 2019-03-05 | 2019-06-14 | 肥城金塔机械有限公司 | Low-concentration ethanol recyclable device and method based on MVR |
| CN110755867A (en) * | 2019-11-16 | 2020-02-07 | 山东众兴泽辉新材料股份有限公司 | Dmf waste liquid treatment device and treatment method thereof |
| CN114593615A (en) * | 2022-03-23 | 2022-06-07 | 上海谋基实业有限公司 | Energy recycling method for acrylic acid purification process |
| CN115253350B (en) * | 2022-08-05 | 2024-08-06 | 淄博万华机械设备有限公司 | Double-tower MVR continuous distillation recovery system and method |
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| CN204522354U (en) * | 2015-01-27 | 2015-08-05 | 湖南百利工程科技股份有限公司 | Solvent refining unit in a kind of synthetic rubber production process |
| CN205598688U (en) * | 2016-04-22 | 2016-09-28 | 常州博睿杰能环境技术有限公司 | Hot integrated system of separated MVR heat pump rectification |
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