CN105964005A - Split type MVR heat pump rectification heat integration system - Google Patents
Split type MVR heat pump rectification heat integration system Download PDFInfo
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- CN105964005A CN105964005A CN201610256631.9A CN201610256631A CN105964005A CN 105964005 A CN105964005 A CN 105964005A CN 201610256631 A CN201610256631 A CN 201610256631A CN 105964005 A CN105964005 A CN 105964005A
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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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- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a split type MVR heat pump rectification heat integration system including a feed preheating part, a circulation part, an upper tower rectification part, a compression-condensation part, a water spray part, a lower tower rectification part, a water steam heating part, a product discharging part, a condensate water discharging part, a kettle liquid discharging part, and a cooling part. The system can be used for some special separation processes with large temperature difference; the system directly compresses gas coming out from a tower top of the upper tower rectification tower, and increases the tower top gas pressure and condensing temperature; the gas is used as a heat source of an upper tower reboiler of the upper tower rectification tower, the condensation latent heat of the compressed gas is fully used, and at the same time, consumption of tower kettle heat utilities and tower top cold utilities is reduced. Compared with traditional rectification, the adopted form is more economical, saves more energy, is moderate in investment cost and simple to control, only a small amount of lowest-level water steam is consumed, and a lot of higher-level water steam can be saved; the process system can produce great economic benefits.
Description
Technical field
The present invention relates to the energy-efficient Technology of one in industry rectification field, use and directly compress overhead gas, and
Main distillation column is divided into the mode of upper and lower two towers, is applied to big temperature difference separation process, to reduce disappearing of steam
Consume and carry out energy-conservation.
Background technology
At present, industry distillation operation uses multi-effect distillation, and due to the increase with effect number, heating steam consumption minimizing produces
Energy-saving effect starts constantly to decline, and is limited by first order heating steam pressure and final stage cooling medium kind, and operation is more
Feel sleepy difficulty, the most also affected by factors such as the character of separation mixture, volatile components content, technological processes；It is correlated with
Energy-conservation having reached capacity, along with the continuous expansion of yield, its energy consumption is the hugest.
Chinese scholars is imitated the aspect such as number, charge order, feed entrance point, heat-exchange network in the rectification of rectification and has been done and grind in a large number
Study carefully, it is proposed that a lot of prioritization schemes, reached certain energy-saving effect.But, multi-effect distillation still suffer from some shortcomings it
Place:
(1) if multi-effect distillation is by arranging the different rectifying column of dry run pressure, the steam of each column overhead of cascade utilization,
But, the rectifying column overhead vapours that operation pressure is minimum needs for using a large amount of circulating water, meanwhile must consume
A large amount of steam carry out the tower bottom of rectifying tower liquid that heating operation pressure is the highest, cause the dual consumption of hot and cold public work；
(2) in multi-effect distillation, the operation temperature of each tower tower reactor raises along with the rising of operation pressure, needs multiple pressure
The fresh water steam of grade is as thermal source；
(3) nominal increase rectification effect number can be more energy-conservation, but this is limited by full factory water vapor levels, Er Qiesui
Operation pressure to improve, the relative volatility of material diminishes, and required reflux ratio is bigger, increases the energy-saving effect of rectification effect number
Become inconspicuous.
CN103285615B and CN103566612B all discloses a kind of conventional formula heat pump rectification system.From Technological Economy
Angle considers, the occasion that conventional heat pump rectification is generally only applicable at the bottom of tower and the tower top temperature difference is less, this temperature difference is the least, required
Work done during compression the least, hot pump performance is better.For big temperature difference separation process (such as methanol, DMAC that some are special
Rectification), use separated heat pump distillation flow process more economically, this flow process takes tower to install heat pump and lower tower reduces back
The conservation measures of flow, energy-saving effect is obvious, and investment cost is moderate, controls simple.
Summary of the invention
The technical problem to be solved is: overcome the deficiency that prior art exists, and proposes one more energy-efficient
Partition type MVR heat pump distillation be thermally integrated system.
In order to solve above-mentioned technical problem, the technical scheme is that a kind of partition type MVR heat pump distillation is thermally integrated
System, described system includes feeding preheating part, upper tower rectification part, cyclic part, compression condensation part, water spray portion
Point, lower tower rectification part, steam heating part, product discharge part, condensed water discharge part, still liquid discharge part,
Cooling segment；
Described feeding preheating part is connected with upper tower rectification part, and upper tower rectification part is connected with cyclic part, compression
Condensation portion is connected with upper tower rectification part, and water emitting portion is connected with compression condensation part, and lower tower rectification part is with upper
Tower rectification part is connected, and steam heating part is connected with upper tower rectification part, lower tower rectification part respectively, product
Discharge part is connected with feeding preheating part, compression condensation part respectively, condensed water discharge part the most respectively with upper tower rectification
Partly, lower tower rectification part, feeding preheating part be connected, still liquid discharge part the most respectively with lower tower rectification part, charging
Regenerator section is connected, and cooling segment is connected with compression condensation part.
Further, described feeding preheating part includes the feed supplement pump (P01) being sequentially connected with, feed storage tank (R01), feeds
Pump (P02), upper tower feed flow meter (FI01), one-level preheater (E01), two grades of preheaters (E02), three grades pre-
Hot device (E03), upper tower rectifying column (T01), lower tower rectifying column (T02)；Described feeding preheating part through one, two,
Material liquid is preheating to bubble point by three grades of preheaters, feeds supreme tower rectifying column (T01) and carries out normal rectification separation, and enters
Expect to lower tower rectifying column (T02) to be served only for feed supplement when system is initially driven, control to feed supreme tower by valve (V01)
Rectifying column (T01), controls charging to lower tower rectifying column (T02) by valve (V02).
Further, described upper tower rectification part includes upper tower rectifying column (T01) and concurrent heating separation chamber (E05) being sequentially connected with；
Described upper tower rectifying column (T01) is plate column rectification separation equipment or packed tower rectification separation equipment or hypergravity rectifier；
Described concurrent heating separation chamber (E05) is the overall separation chamber with concurrent heating function or the separate separation with external heat device
Room.
Further, described cyclic part includes being sequentially connected with concurrent heating separation chamber (E05), upper tower circulating pump (P04), on
Tower reboiler (E06)；Described upper tower reboiler (E06) be shell and tube reboiler or spiral plate type reboiler or board-like again
Boiling device or spiral winded type reboiler.
Further, described compression condensation part includes the upper tower rectifying column (T01) being sequentially connected with, compressor (C01), satisfies
With device (R02), upper tower reboiler (E06), product surge tank (R03)；Described compressor (C01) is centrifugal pressure
Contracting machine or Roots Compressor or screw compressor；Described saturator (R02) bottom is provided with a water seal arrangement, is
Unnecessary injection flow rate of uniting flows into product surge tank (R03) after water seal arrangement.
Further, described water emitting portion includes the product surge tank (R03) being sequentially connected with, upper tower discharge pump (P06), sprays
Water ga(u)ge (FI03), saturator (R02), product surge tank (R03).
Further, described lower tower rectification part includes the lower tower feed pump (P05) being sequentially connected with, lower tower feed flow meter
(FI02), lower tower rectifying column (T02), lower tower reboiler (E04)；Described lower tower feed pump (P05) is afterwards by valve (V05)
Control to feed to lower tower rectifying column (T02), control to be back to upper tower rectifying column (T01) by valve (V06)；Under described
Tower rectifying column (T02) carries out Natural Circulation with lower tower reboiler (E04) and separates.
Further, described steam heating part includes being sequentially connected with raw vapour source, lower tower reboiler (E04), concurrent heating
Separation chamber (E05).
Further, described product discharge part includes being sequentially connected with upper tower discharge pump (P06), one-level preheater (E01),
Product stream gauge (FI05), finished product storage tank (R04), finished product unloading pump (P07) and return flow meter (FI04),
Upper tower rectifying column (T01)；Described product stream gauge (FI05) is adjusted by valve (V11), described return flow
Meter (FI04) is adjusted by valve (V10).
Further, described condensed water discharge part includes condensate pump (P08), the condensation flow gauge being sequentially connected with
(FI06), two grades of preheaters (E02).
Further, described still liquid discharge part includes being sequentially connected with lower tower reactor liquid pump (P03), still flow meters (FI07),
Three grades of preheaters (E03), still liquid storage tanks (R05)；Described still flow meters (FI07) is adjusted by valve (V04)
Joint.
Further, described cooling segment includes the product surge tank (R03) being sequentially connected with, gas condenser (E07), enters
Material storage tank (R01), and cooling water storage tank (R06), cooling water pump (P10), cooling water flow meter (FI08)；Institute
State gas condenser (E07) condensate outlet pipeline and need fully-inserted feed storage tank (R01) is formed fluid-tight.
After have employed technique scheme, the method have the advantages that
(1) this system is than other system more science, more energy-efficient, have operating cost low, easy to adjust,
Steady operation and other merits；
(2) this system can be full recycled to receive and utilize such as methanol, ethanol, isopropanol, DMAC, DMF, DMSO
Energy-conservation purpose is reached Deng the indirect steam in the big temperature difference separation process that some are special；
(3) this system directly compresses tower top gas out, takes full advantage of by the condensation latent heat of compressed gas, simultaneously
Reduce the hot public work of tower reactor and the consumption of the cold public work of tower top；
(4) considering from Technological Economy angle, using separated heat pump distillation flow process more economically, this flow process is taked
Tower installs heat pump and the conservation measures of lower tower reduction capacity of returns, and energy-saving effect is obvious, and investment cost is moderate, controls simple；
(5) for relatively conventional rectification, use this form more economically, energy-conservation, investment cost is moderate, controls simple,
Only need to consume the steam (such as 0.3MPa) of a small amount of lowest level, save simultaneously a large amount of greater degree steam (as
1.0MPa), it is possible to produce huge economic benefit.
Accompanying drawing explanation
In order to be illustrated more clearly that the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
In technology description, the required accompanying drawing used is briefly described, it should be apparent that, the accompanying drawing in describing below is only originally
Some embodiments of invention, for those of ordinary skill in the art, on the premise of not paying creative work, also
Other accompanying drawing can be obtained according to these accompanying drawings.
Fig. 1 is the process chart that a kind of partition type MVR heat pump distillation of the present invention is thermally integrated system；
Fig. 2 is the process chart of single tower distillation；
Fig. 3 is the process chart of double-effect rectification；
Fig. 4 is the process chart of single column heat pump distillation；
In figure, code name is expressed as follows respectively:
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), still liquid unloading pump (P09),
Cooling water pump (P10)；One-level preheater (E01), two grades of preheaters (E02), three grades of preheaters (E03), lower towers
Reboiler (E04), concurrent heating separation chamber (E05), upper tower reboiler (E06), gas condenser (E07)；Charging storage
Tank (R01), saturator (R02), product surge tank (R03), finished product storage tank (R04), still 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), product stream gauge (FI05), condensation flow gauge (FI06), still flow meters (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).
Detailed description of the invention
It is clearly understood to make present disclosure be easier to, below according to specific embodiment and combine accompanying drawing, to this
Invention is described in further detail.
As it is shown in figure 1, a kind of partition type MVR heat pump distillation is thermally integrated system, described system include feeding preheating part,
Upper tower rectification part, cyclic part, compression condensation part, water emitting portion, lower tower rectification part, steam heating part,
Product discharges part, condensed water discharges part, still liquid discharges part, cooling segment；
Described feeding preheating part is connected with upper tower rectification part, and upper tower rectification part is connected with cyclic part, compression
Condensation portion is connected with upper tower rectification part, and water emitting portion is connected with compression condensation part, and lower tower rectification part is with upper
Tower rectification part is connected, and steam heating part is connected with upper tower rectification part, lower tower rectification part respectively, product
Discharge part is connected with feeding preheating part, compression condensation part respectively, condensed water discharge part the most respectively with upper tower rectification
Partly, lower tower rectification part, feeding preheating part be connected, still liquid discharge part the most respectively with lower tower rectification part, charging
Regenerator section is connected, and cooling segment is connected with compression condensation part.
Preferably, as it is shown in figure 1, described feeding preheating part includes feed supplement pump (P01), the feed storage tank being sequentially connected with
(R01), feed pump (P02), upper tower feed flow meter (FI01), one-level preheater (E01), two grades of preheaters (E02),
Three grades of preheaters (E03), upper tower rectifying column (T01), lower tower rectifying columns (T02)；Described feeding preheating part is passed through
Material liquid is preheating to bubble point by one, two, three preheater, feeds supreme tower rectifying column (T01) and carries out normal rectification and divide
From, and feed to lower tower rectifying column (T02) and be served only for feed supplement when system is initially driven, by valve (V01) control into
Expect supreme tower rectifying column (T01), control charging to lower tower rectifying column (T02) by valve (V02).
Preferably, as it is shown in figure 1, described upper tower rectification part includes the upper tower rectifying column (T01) being sequentially connected with and mends
Thermal release room (E05)；Described upper tower rectifying column (T01) is plate column rectification separation equipment, naturally it is also possible to for filler
The rectification separation equipment of the forms such as tower rectification separation equipment or hypergravity rectifier；Described concurrent heating separation chamber (E05) is whole
The separation chamber with concurrent heating function of body, it is also possible to for the separate separation chamber with external heat device.
Preferably, as it is shown in figure 1, described cyclic part includes the concurrent heating separation chamber (E05) being sequentially connected with, the circulation of upper tower
Pump (P04), upper tower reboiler (E06)；Described upper tower reboiler (E06) is shell and tube reboiler, naturally it is also possible to
For spiral plate type reboiler or the reboiler of the form such as board-like reboiler or spiral winded type reboiler.
Preferably, as it is shown in figure 1, described compression condensation part includes upper tower rectifying column (T01), the compression being sequentially connected with
Machine (C01), saturator (R02), upper tower reboiler (E06), product surge tank (R03)；Described compressor (C01)
For centrifugal compressor, can also be Roots Compressor or screw compressor certainly；Described saturator (R02) end
Portion is provided with a water seal arrangement, and the unnecessary injection flow rate of system flows into product surge tank (R03) after water seal arrangement.
Preferably, as it is shown in figure 1, described water emitting portion includes the product surge tank (R03) being sequentially connected with, upper tower finished product
Pump (P06), water jet gauge (FI03), saturator (R02), product surge tank (R03)；Described water emitting portion master
Superheated steam to be used for eliminates the degree of superheat.
Preferably, as it is shown in figure 1, described lower tower rectification part includes the lower tower feed pump (P05) being sequentially connected with, lower tower
Feed flow meter (FI02), lower tower rectifying column (T02), lower tower reboiler (E04)；Described lower tower feed pump (P05)
Control to feed to lower tower rectifying column (T02) by valve (V05) afterwards, control to be back to upper tower rectification by valve (V06)
Tower (T01), described valve (V06) is served only for when system is initially driven refluxing；Described lower tower rectifying column (T02) with under
Tower reboiler (E04) carries out Natural Circulation separation.
Preferably, as it is shown in figure 1, described steam heating part includes the raw vapour source being sequentially connected with, lower tower reboiler
(E04), concurrent heating separation chamber (E05)；It is mainly used in heating and lower tower reboiler (E04) to concurrent heating separation chamber
(E05) concurrent heating is carried out.
Preferably, as it is shown in figure 1, described product discharge part includes upper tower discharge pump (P06), the one-level being sequentially connected with
Preheater (E01), product stream gauge (FI05), finished product storage tank (R04), finished product unloading pump (P07) and backflow stream
Gauge (FI04), upper tower rectifying column (T01)；Described product stream gauge (FI05) is adjusted by valve (V11),
Described return flow meter (FI04) is adjusted by valve (V10).
Preferably, as it is shown in figure 1, described condensed water discharge part includes condensate pump (P08), the condensation being sequentially connected with
Water ga(u)ge (FI06), two grades of preheaters (E02).
Preferably, as it is shown in figure 1, described still liquid discharge part includes lower tower reactor liquid pump (P03), the still liquid being sequentially connected with
Effusion meter (FI07), three grades of preheaters (E03), still liquid storage tanks (R05)；Described still flow meters (FI07) is passed through
Valve (V04) is adjusted, and described valve (V03) is served only for when system is initially driven feeding concurrent heating separation chamber (E05)
Time use.
Preferably, as it is shown in figure 1, described cooling segment includes product surge tank (R03), the gas condensation being sequentially connected with
Device (E07), feed storage tank (R01), and cooling water storage tank (R06), cooling water pump (P10), cooling water flow
Meter (FI08)；Described gas condenser (E07) condensate outlet pipeline needs in fully-inserted feed storage tank (R01)
Form fluid-tight.
The operation principle of the present invention is as follows:
The main distillation column of separated heat pump distillation flow process is divided into upper and lower two towers: upper tower is similar to conventional heat pump rectification, the most
One charging aperture；And lower tower is similar to the stripping section of conventional rectification, feeding the still liquid from upper tower, steam discharging is then entered
Enter at the bottom of upper tower tower.The upper tower temperature difference can be made smaller by controlling cut-point concentration (i.e. descending tower input concentration), thus reduce
Compression ratio needed for compressor, reduces investment and operating cost, shortens the payoff period of additional investment.Upper tower is installed heat pump and can be taken
Obtaining preferable effect, coefficient COP is bigger for heat pump heat supply；Meanwhile, the capacity of returns of lower tower also can be greatly reduced, steam
Consume and reduce.
Preferably, the feed supplement pump (P01) of described system carries out feed supplement, feed pump (P02) to feed storage tank (R01)
Feed after upper tower feed flow meter (FI01) carries out flow-control from feed storage tank (R01), use the product discharged
After product carry out one-level preheating by one-level preheater (E01) to material liquid, use the condensed water discharged by two grades of preheatings
After device (E02) carries out two grades of preheatings to material liquid, use the still liquid discharged by three grades of preheaters (E03) to material liquid
After carrying out three grades of preheatings, reach bubble point temperature and be directly entered tower rectifying column (T01) and carry out rectifying section purification operations.
In described entrance, the material liquid of tower rectifying column (T01) carries out being uniformly distributed tailing edge tower with liquid phase state from upper therein
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 essence
Evaporate tower (T02) to feed, equally along tower with the top-down tower bottom that flow to of liquid phase state, and lower tower rectifying column (T02)
The liquid of bottom carries out Natural Circulation evaporation by lower tower rectifying column (T02) with lower tower reboiler (E04) and separates, and makes
Lower tower reboiler (E04) is heated, after tower bottoms reaches the concentration of emission request, by lower tower with raw steam
Still liquid pump (P03) carries out discharge, uses still flow meters (FI07) to carry out flow-control, pre-subsequently into three grades
Hot device (E03) carries out three grades of preheatings to material liquid, and is collected in still liquid storage tank (R05), uses still liquid after filling liquid
Unloading pump (P09) shifts.
Condensed fluid after upper tower rectifying column (T01) is heated by described raw steam with lower tower reboiler (E04) passes through cold
Condensate pump (P08) carries out discharge opeing, uses condensation flow gauge (FI06) to carry out flow-control, subsequently into two grades
After preheater (E02) carries out two grades of preheatings to material liquid, carry out outer row.
Preferably, the lower tower rectifying column (T02) of described system and lower tower reboiler (E04) carry out Natural Circulation evaporation point
From the saturated gas obtained then along tower with gas phase state from bottom to top flow to top of tower, and enter with top-down liquid phase state
Row gas-liquid mass transfer separates, and is finally reached gas-liquid phase equilibrium process；From lower tower rectifying column (T02) top of tower out after full
After entering concurrent heating separation chamber (E05) with gas, divide with from concurrent heating separation chamber (E05) and upper tower reboiler (E06)
The saturated gas separated out together along upper tower rectifying column (T01) with gas phase state from bottom to top from top of tower flow out, equally
Carry out gas-liquid mass transfer with top-down liquid phase state to separate, be finally reached gas-liquid phase equilibrium process.
The described saturated gas flowed out from upper tower rectifying column (T01) top of tower enters compressor (C01) and is compressed acting
After, the pressure and temperature of overhead gas is improved, and becomes superheated steam, enters saturator (R02) and carries out eliminating
Temperature, and become saturated vapor, subsequently enter and tower reboiler (E06) carries out heat transfer condensation, after becoming liquid,
It is collected in product surge tank (R03), is shunted by upper tower discharge pump (P06)；A part of liquid passes through finished product
After effusion meter (FI05) carries out flow-control, enter in saturator (R02) mistake out from compressor (C01)
Vapours carries out eliminating the degree of superheat；Another part liquid then enters one-level preheater (E01), and that material liquid is carried out one-level is pre-
After heat, again shunt, after a part of liquid carries out flow-control by return flow meter (FI04), be back to
Tower rectifying column (T01) carries out gas-liquid mass transfer separation process, and to improve product purity further, another part liquid is then
After carrying out flow-control by product stream gauge (FI05), it is collected in finished product storage tank (R04), uses after filling liquid
Finished product unloading pump (P07) shifts.
Unnecessary hydrojet in described entrance saturator (R02), after being collected in saturator (R02) bottom, by arranging
Fluid-tight and be back to product surge tank (R03).
Liquid in described concurrent heating separation chamber (E05) is by tower reboiler (E06) in the entrance of upper tower circulating pump (P04)
In heat and after evaporating, entering concurrent heating separation chamber (E05) carries out flash distillation and isolated product saturated gas, this
Process is forced circulation process.
Preferably, the saturated gas or the incoagulable gas that are not condensed in described ready system products surge tank (R03) enter
Enter after gas condenser (E07) condenses, enter in feed storage tank (R01), described gas condenser (E07)
Condensate outlet pipeline needs to be formed in fully-inserted feed storage tank (R01) fluid-tight.Described cooling water enters cooling water storage
Tank (R06), subsequently into cooling water pump (P10), after carrying out flow-control by cooling water flow meter (FI08), enters
Enter the gas condenser (E07) saturated gas to not being condensed or incoagulable gas cools down, then arrange
Put.
In actual production, as a example by producing 600000 tons of methanol per year, use partition type MVR heat pump distillation heat as shown in Figure 1
The process chart of integrated system.When feed conditions is 61.8 ten thousand tons, produces by 8000 hours every year, charging
Temperature is 71.6 DEG C, and feed rate is 94277kg/h, and feed pressure is 1.7MPaG, feed composition be methanol 82%,
Water 18%；Tower top requires as methanol 96.8%, water 3.2%；Tower reactor requires as methanol 0.1%, water 99.9%；Ta Neita
Anode drop is 0.7kPa.
Comparative example:
Equally as a example by producing 600000 tons of methanol per year, employing process chart as shown in Figure 2, Figure 3, Figure 4, but other
Operating parameter is the most identical.
Embodiment is compared with comparative example, and energy consumption and cost parameter contrast table are as shown in table 1, steam and electricity consumption are all converted to
Mark coal, compares total conversion mark coal, double-effect rectification energy-conservation relative to single tower distillation 18.9%, single column heat pump distillation phase
Energy-conservation for single tower distillation 76.48%, separated heat pump distillation energy-conservation relative to single tower distillation 75.28%, single column heat pump essence
Evaporate energy-conservation relative to double-effect rectification 70.98%, separated heat pump distillation energy-conservation relative to double-effect rectification 69.49%.By steam
Electricity price lattice, according to market price 120 yuan/ton, are carried out being converted to total price according to market price 0.8 yuan/degree and compare by price,
Double-effect rectification cost-effective relative to single tower distillation 18.98%, single column heat pump distillation is cost-effective relative to single tower distillation
-38.49%, separated heat pump distillation cost-effective relative to single tower distillation 46.99%, single column heat pump distillation is relative to economic benefits and social benefits
Rectification cost-effective-70.93%, separated heat pump distillation cost-effective relative to double-effect rectification 34.57%.
Table 1 energy consumption and cost parameter contrast table
By embodiment compared with comparative example, for current industrial distillation technology, use segmentation as shown in Figure 1
Formula MVR heat pump distillation is thermally integrated the process chart of system than the process chart used as shown in Figure 2, Figure 3, Figure 4
Time, the most energy-conservation, production cost is lower.
This system is than other system more science, more energy-efficient, has that operating cost is low, easy to adjust, work is steady
The advantage such as fixed；
This system can be full recycled to receive and utilize such as methanol, ethanol, isopropanol, DMAC, DMF, DMSO etc.
Indirect steam in some special big temperature difference separation processes and reach energy-conservation purpose；
This system directly compresses tower top gas out, takes full advantage of by the condensation latent heat of compressed gas, reduces simultaneously
The hot public work of tower reactor and the consumption of the cold public work of tower top；
Considering from Technological Economy angle, using separated heat pump distillation flow process more economically, this flow process takes tower to install
Heat pump and lower tower reduce the conservation measures of capacity of returns, and energy-saving effect is obvious, and investment cost is moderate, control simple；
For relatively conventional rectification, use this form more economically, energy-conservation, investment cost is moderate, controls simple, only needs
Consume the steam (such as 0.3MPa) of a small amount of lowest level, save the steam of a large amount of greater degree (such as 1.0 simultaneously
MPa), it is possible to produce huge economic benefit.
Particular embodiments described above, to present invention solves the technical problem that, technical scheme and beneficial effect entered
One step describes in detail, be it should be understood that the specific embodiment that the foregoing is only the present invention, is not limited to
The present invention, all within the spirit and principles in the present invention, any modification, equivalent substitution and improvement etc. done, all should wrap
Within being contained in protection scope of the present invention.
Claims (12)
1. a partition type MVR heat pump distillation is thermally integrated system, it is characterised in that described system includes feeding preheating portion
Point, upper tower rectification part, cyclic part, compression condensation part, water emitting portion, lower tower rectification part, steam heating
Partly, product discharges part, condensed water discharges part, still liquid discharges part, cooling segment；
Described feeding preheating part is connected with upper tower rectification part, and upper tower rectification part is connected with cyclic part, compression
Condensation portion is connected with upper tower rectification part, and water emitting portion is connected with compression condensation part, and lower tower rectification part is with upper
Tower rectification part is connected, and steam heating part is connected with upper tower rectification part, lower tower rectification part respectively, product
Discharge part is connected with feeding preheating part, compression condensation part respectively, condensed water discharge part the most respectively with upper tower rectification
Partly, lower tower rectification part, feeding preheating part be connected, still liquid discharge part the most respectively with lower tower rectification part, charging
Regenerator section is connected, and cooling segment is connected with compression condensation part.
A kind of partition type MVR heat pump distillation the most according to claim 1 is thermally integrated system, it is characterised in that institute
State feed supplement pump (P01) that feeding preheating part includes being sequentially connected with, feed storage tank (R01), feed pump (P02), upper tower
Feed flow meter (FI01), one-level preheater (E01), two grades of preheaters (E02), three grades of preheaters (E03), on
Tower rectifying column (T01), lower tower rectifying column (T02)；Described feeding preheating part passes through one, two, three preheater by former
Feed liquid is preheating to bubble point, feeds supreme tower rectifying column (T01) and carries out normal rectification separation, and is controlled by valve (V01)
System feeds supreme tower rectifying column (T01), controls charging to lower tower rectifying column (T02) by valve (V02).
A kind of partition type MVR heat pump distillation the most according to claim 2 is thermally integrated system, it is characterised in that institute
State upper tower rectifying column (T01) and concurrent heating separation chamber (E05) that tower rectification part includes being sequentially connected with；Described upper tower essence
Evaporating tower (T01) is plate column rectification separation equipment or packed tower rectification separation equipment or hypergravity rectifier；Described concurrent heating
Separation chamber (E05) is the overall separation chamber with concurrent heating function or the separate separation chamber with external heat device.
A kind of partition type MVR heat pump distillation the most according to claim 3 is thermally integrated system, it is characterised in that institute
State concurrent heating separation chamber (E05) that cyclic part includes being sequentially connected with, upper tower circulating pump (P04), upper tower reboiler (E06)；
Described upper tower reboiler (E06) is shell and tube reboiler or spiral plate type reboiler or board-like reboiler or spiral winded type
Reboiler.
A kind of partition type MVR heat pump distillation the most according to claim 4 is thermally integrated system, it is characterised in that institute
State upper tower rectifying column (T01) that compression condensation part includes being sequentially connected with, compressor (C01), saturator (R02),
Upper tower reboiler (E06), product surge tank (R03)；Described compressor (C01) is centrifugal compressor or roots-type
Compressor or screw compressor；Described saturator (R02) bottom is provided with a water seal arrangement, the unnecessary injection flow rate of system
Product surge tank (R03) is flowed into after water seal arrangement.
A kind of partition type MVR heat pump distillation the most according to claim 5 is thermally integrated system, it is characterised in that institute
State product surge tank (R03) that water emitting portion includes being sequentially connected with, upper tower discharge pump (P06), water jet gauge (FI03),
Saturator (R02), product surge tank (R03).
A kind of partition type MVR heat pump distillation the most according to claim 6 is thermally integrated system, it is characterised in that institute
State lower tower feed pump (P05) that lower tower rectification part includes being sequentially connected with, lower tower feed flow meter (FI02), lower tower essence
Evaporate tower (T02), lower tower reboiler (E04)；Described lower tower feed pump (P05) controls charging by valve (V05) afterwards
To lower tower rectifying column (T02), control to be back to upper tower rectifying column (T01) by valve (V06)；Described lower tower rectifying column
(T02) carry out Natural Circulation with lower tower reboiler (E04) to separate.
A kind of partition type MVR heat pump distillation the most according to claim 7 is thermally integrated system, it is characterised in that institute
State raw vapour source that steam heating part includes being sequentially connected with, lower tower reboiler (E04), concurrent heating separation chamber (E05).
A kind of partition type MVR heat pump distillation the most according to claim 8 is thermally integrated system, it is characterised in that institute
State upper tower discharge pump (P06) that product discharge part includes being sequentially connected with, one-level preheater (E01), product stream gauge
(FI05), finished product storage tank (R04), finished product unloading pump (P07) and return flow meter (FI04), upper tower rectifying column
(T01)；Described product stream gauge (FI05) is adjusted by valve (V11), described return flow meter (FI04)
It is adjusted by valve (V10).
A kind of partition type MVR heat pump distillation the most according to claim 9 is thermally integrated system, it is characterised in that
Condensate pump (P08) that described condensed water discharge part includes being sequentially connected with, condensation flow gauge (FI06), two grades pre-
Hot device (E02).
11. a kind of partition type MVR heat pump distillations according to claim 10 are thermally integrated system, it is characterised in that
Lower tower reactor liquid pump (P03) that described still liquid discharge part includes being sequentially connected with, still flow meters (FI07), three grades of preheatings
Device (E03), still liquid storage tank (R05)；Described still flow meters (FI07) is adjusted by valve (V04).
12. a kind of partition type MVR heat pump distillations according to claim 11 are thermally integrated system, it is characterised in that
Product surge tank (R03) that described cooling segment includes being sequentially connected with, gas condenser (E07), feed storage tank (R01),
And cooling water storage tank (R06), cooling water pump (P10), cooling water flow meter (FI08)；Described gas condenser (E07)
Condensate outlet pipeline needs to be formed in fully-inserted feed storage tank (R01) fluid-tight.
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| CN107583300A (en) * | 2017-10-16 | 2018-01-16 | 中国科学院理化技术研究所 | A kind of hypergravity MVR heat pump rectification systems |
| CN108079610A (en) * | 2018-01-15 | 2018-05-29 | 苏州欧拉透平机械有限公司 | Energy-saving methanol rectifying system and its rectificating method |
| 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 |
| CN115253350A (en) * | 2022-08-05 | 2022-11-01 | 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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| CN105964005B (en) | 2018-04-17 |
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Effective date of registration: 20200929 Address after: Room 550, 5 / F, block a, Chuangye building, Guiyuan Avenue, Nanchang Economic and Technological Development Zone, Nanchang City, Jiangxi Province Patentee after: Jiangxi kemiaode Pharmaceutical Technology Co., Ltd Address before: 213031 Jiangsu province Changzhou City New District Chang Cheng Road, No. 888 Patentee before: CHANGZHOU BRIGENIUS ENERGY & ENVIRONMENT TECH Co.,Ltd. |