CN107935825A - Polymethoxy dimethyl ether refining spearation system and the method that polymethoxy dimethyl ether is prepared using the system - Google Patents
Polymethoxy dimethyl ether refining spearation system and the method that polymethoxy dimethyl ether is prepared using the system Download PDFInfo
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- CN107935825A CN107935825A CN201711459839.1A CN201711459839A CN107935825A CN 107935825 A CN107935825 A CN 107935825A CN 201711459839 A CN201711459839 A CN 201711459839A CN 107935825 A CN107935825 A CN 107935825A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
Abstract
A kind of method that polymethoxy dimethyl ether is prepared the invention discloses polymethoxy dimethyl ether refining spearation system and using the system, belongs to polymethoxy dimethyl ether refining spearation technical field.The refining spearation system includes sequentially connected rough system, refining system and impurity removed system.The present invention by the separation of DMM3 4 and DMM5 8, makes product diversification by refining system, and use scope is more extensive, and the present invention reduces the use of quantity of steam, saved cost by the use of material heat in itself as the heat source of reboiler.
Description
Technical field
The present invention relates to polymethoxy dimethyl ether refining spearation technical field, and in particular to a kind of polymethoxy dimethyl ether essence
Piece-rate system processed and the method that polymethoxy dimethyl ether is prepared using the system.
Background technology
DMMn (polymethoxy dimethyl ether) is the novel environment-friendly for reducing oil consumption and reducing flue gas emission generally acknowledged in the world
Fuel oil reconciliation component, Cetane number height (80~100CN), low temperature flow is good, can improve the combustibility of diesel oil, reduces vapour
The discharge of tail gas.DMMn physical property is close with diesel oil, be blended into diesel oil be used without to vehicle motor oil supply system into
Row transformation.External major company carries out R and D to the production technology of DMMn in succession, is shown by experiment and application study：Add
Add 20% this oxycompound, smoke intensity highest, which can reduce by 80%~90%, NOx, can reduce by 50%, while the thermal efficiency also compares
Present alone diesel oil will height.
So far production DMMn uses distillation technology, but energy consumption is higher need to further change technological process, just reaches energy saving drop
The purpose of consumption.In addition, also useful benzene extraction is separated, the drawback is that benzene is extremely toxic substance, it is not completely separated after extraction dry
Only, cause to contain benzene in product, have greater environmental impacts, and benzene extraction process flow is longer, and energy consumption is higher, waste water yield
Greatly, and intractability containing benzene is larger in waste water.
DMMn products component is DMM2, DMM3, DMM4, DMM5, DMM6, DMM7, DMM8 and heavy constituent.Wherein, DMM2 is produced
Product existing process can be kept completely separate, but DMM3-8 is mixture, can not be kept completely separate.
The content of the invention
Prepared it is an object of the invention to provide a kind of polymethoxy dimethyl ether refining spearation system and using the system poly-
The method of methoxyl group dimethyl ether, to solve, existing DMMn isolation technics separating effect is bad, can not realize DMMn product diversification
And cost it is higher the problem of.
The technical solution that the present invention solves above-mentioned technical problem is as follows：
A kind of polymethoxy dimethyl ether refining spearation system, including：Sequentially connected rough system, refining system and removal of impurities
System；
Rough system includes product tower, the first reboiler and DMM2 product storage tanks；First reboiler is arranged at product tower
Bottom of towe section, the top material outlet of product tower are connected with DMM2 product storage tanks, and the bottoms material outlet of product tower passes through the first tower
Kettle discharging pump is connected to refining system；
Refining system includes treating column, the second reboiler, precools equipment, tower top by flow container and with precooling equipment company
The steam jet pump connect；Second reboiler is arranged at the bottom of towe section for the treatment of column；Material inlet and product tower in the middle part for the treatment of column
Bottoms material outlet connection, the top material outlet for the treatment of column are connected with precooling equipment, tower top by flow container successively, treating column
Bottoms material outlet is divided into two bye-passes, and one of bye-pass is connected to the second reboiler by reboiler circulation pump, separately
One bye-pass is connected to DMM5-8 product storage tanks by the second tower reactor discharging pump；Tower top is connected with the second tower by the outlet of flow container
Discharging pump is pushed up, the outlet of the second tower top discharging pump is divided into two bye-passes, and the tower top section of one of bye-pass and treating column is returned
Head piece connects, another bye-pass is connected to impurity removed system.
Further, in preferred embodiments of the present invention, above-mentioned precooling equipment is cold including the first cooler and second
But the top material outlet of device, the entrance of the first cooler and treating column connects, the outlet of the first cooler respectively with tower top by
The entrance of flow container and the second cooler connects, and the outlet of the second cooler is connected with tower top by the entrance of flow container.
Further, in preferred embodiments of the present invention, above-mentioned refining system further includes tower top discharging cooler, tower top
Discharging cooler is arranged on the bye-pass between the second tower top discharging pump and impurity removed system.
Further, in preferred embodiments of the present invention, above-mentioned refining system further includes tower reactor discharging cooler, tower reactor
Discharging cooler is arranged on the bye-pass between the second tower reactor discharging pump and DMM5-8 product storage tanks.
Further, in preferred embodiments of the present invention, the entrance of above-mentioned first tower reactor discharging pump and the bottom of product tower
Portion's material outlet connection, the outlet of the first tower reactor discharging pump are divided into two bye-passes, the tower of one of bye-pass and product tower
The material inlet of bottom section refluxing opening connection, another bye-pass and treating column connects.
Further, in preferred embodiments of the present invention, above-mentioned rough system further includes the first tower top discharging pump, and first
The entrance of tower top discharging pump is connected with the material outlet of DMM2 product storage tanks, and the outlet of the first tower top discharging pump is divided into two branch pipes
Road, one of bye-pass are connected with the tower top section refluxing opening of product tower, another bye-pass is connected to DMM2 rectifying columns.
Further, in preferred embodiments of the present invention, above-mentioned impurity removed system includes the first adsorption tanks in parallel and the
The entrance of two adsorption tanks, the first adsorption tanks and the second adsorption tanks is connected with tower top by the outlet of flow container, the first adsorption tanks and
The outlet of two adsorption tanks is connected with DMM3-4 product storage tanks.
The method for preparing polymethoxy dimethyl ether using above-mentioned polymethoxy dimethyl ether refining spearation system, including：
(1) the DMM2-8 products from lightness-removing column are delivered in product tower, by distillation, isolated DMM2 is produced
Product are exported to DMM2 product storage tanks from product top of tower, and isolated DMM3-8 products are exported to refined from product tower bottom
Tower；Wherein, the operation temperature of product tower is 138 DEG C；
(2) rectifying in treating column by DMM3-8 products, isolated DMM3-4 products are exported at the top for the treatment of column
40 DEG C are cooled to precooling in equipment, isolated DMM5-8 products are exported from refined tower bottom, DMM5-8 products go out
Material is divided into two strands, and wherein one returns again to treating column under the action of reboiler circulation pump after the utilization of the second reboiler
In, another strand is disclosed as output of products, dress；Wherein, the operation temperature for the treatment of column is 173 DEG C；
(3) DMM3-4 products are subjected to removal of impurities processing in impurity removed system；Wherein, the running temperature of impurity removed system is not higher than
80℃。
Further, in preferred embodiments of the present invention, step (2) includes step in detail below：
(21) before start, the pipeline and pump for the treatment of column is preheated, are preheated to 75-80 DEG C；
(22) the cooling water outlet and inlet valve for precooling equipment is opened, opens steam jet pump, and adjust treating column tower
Interior pressure extremely -94KPa；
(23) treating column is fed, and establishes bottom of towe liquid level；When bottom of towe liquid level accounts for the 20% for the treatment of column volume, second is opened again
Device is boiled, the running temperature for adjusting treating column tower reactor is 170-175 DEG C, and tower top temperature is 95-100 DEG C；Control tower bottom normal operation
Liquid level is account for treating column volume 60%；
(24) the second tower reactor discharging pump is opened when DMM5 contents reach 28% in treating column kettle material, produces DMM5-8
Product；The second tower top discharging pump is opened when the DMM3-4 purity of refined column overhead reaches 99.5%, DMM3-4 products are conveyed
Into impurity removed system.
The invention has the advantages that：
The present invention is separated the DMM3-4 being mingled in DMM3-8 products by treating column, can obtain DMM2, DMM3-
4th, DMM5-8 products so that product diversification, use scope are more extensive；And gone out in separation process using treating column tower reactor
The heat of the DMM5-8 products of material, as the heat source of the second reboiler, product heat is recycled, reduces steaming
Vapour consumption, energy conservation and environmental protection, reduces production cost.
The outlet for being arranged on the respective discharging pump of tower top section and bottom of towe section of rough tower and treating column is divided into two by the present invention
A bye-pass, one of bye-pass of each discharging pump are attached using the connection mode for being back to former tower；Wherein, slightly
First tower top discharging pump of tower processed is connected by bye-pass with rough tower, by unsegregated DMM3-8 products in DMM2 products again
Distillation, so as to improve the purity of DMM2 products；First tower reactor discharging pump of rough tower is connected by bye-pass with rough tower, will
DMM3-8 products, which return again to, carries out distillation reaction in tower reactor, unsegregated a small amount of DMM2 in DMM3-8 products is separated again
Go out, improve production efficiency, while also make it that DMM3-8 products are purer, reduce the residual of DMM2.Second tower for the treatment of column
Top discharging pump is connected by bye-pass with treating column, by unsegregated DMM5-8 products rectifying again in DMM3-4 products, so that
Improve the purity of DMM3-4 products；At the same time by reboiler circulation pump by the DMM5-8 of a portion of tower reactor bottom discharge mouth
Product is pumped to the second reboiler, provides heat source for the second reboiler, reduces steam consumption, treating column is returned again to after heat exchange
In DMM5-8 products can further separating-purifying.
The present invention is cooled down the DMM3-4 products at the top for the treatment of column by cooling device, wherein, the first cooler will
The DMM3-4 vapour phases of tower top be cooled to 65 DEG C be condensed into after liquid flow into it is by flow container, the second cooler that the first cooler is uncooled
Part DMM3-4 vapour phases be further cooled to 25 DEG C and be condensed into after liquid and flow into by flow container.The present invention can by double coolers
Preferably prevent vapour phase from flowing into exhaust system, improve production efficiency.
It is 170-175 DEG C, -94KPa that the present invention, which adjusts the running temperature for the treatment of column and pressure, so that DMM3-8 will be mingled in
DMM3-4 products in product are effectively separated.
Brief description of the drawings
Fig. 1 is the structure diagram of the polymethoxy dimethyl ether refining spearation system of the present invention；
Fig. 2 is the structure diagram of the rough system of the polymethoxy dimethyl ether refining spearation system of the present invention；
Fig. 3 is the structure diagram of the refining system of the polymethoxy dimethyl ether refining spearation system of the present invention；
Fig. 4 is the structure diagram of the impurity removed system of the polymethoxy dimethyl ether refining spearation system of the present invention.
In figure：100- polymethoxy dimethyl ether refining spearation systems；The rough systems of 10-；101- product towers；102- first is again
Boil device；103-DMM2 product storage tanks；104- the first tower top discharging pumps；105- the first tower reactor discharging pumps；20- refining systems；201-
Treating column；The second reboilers of 202-；203- cooling devices；204- tower tops are by flow container；205- steam jet pumps；The second tower tops of 206-
Discharging pump；207- the second tower reactor discharging pumps；208- reboiler circulation pumps；209- tower tops discharging cooler；The discharging of 210- tower reactors is cold
But device；The first coolers of 211-；The second coolers of 212-；30- impurity removed systems；The first adsorption tanks of 301-；The second adsorption tanks of 302-.
Embodiment
The principle and features of the present invention will be described below with reference to the accompanying drawings, and the given examples are served only to explain the present invention, and
It is non-to be used to limit the scope of the present invention.
Embodiment
Fig. 1 is refer to, the polymethoxy dimethyl ether refining spearation system 100 of the embodiment of the present invention includes：It is sequentially connected
Rough system 10, refining system 20 and impurity removed system 30.
Fig. 2 is refer to, rough system 10 includes product tower 101, the first reboiler 102, DMM2 product storage tanks 103, first
104 and first tower reactor discharging pump 105 of tower top discharging pump.First reboiler 102 is arranged at the bottom of towe section of product tower 101.Product tower
101 top material outlet is connected with DMM2 product storage tanks 103, and the bottoms material outlet of product tower 101 is gone out by the first tower reactor
Material pump 105 is connected to refining system 20.The entrance of first tower top discharging pump 104 connects with the material outlet of DMM2 product storage tanks 103
Connect, the outlet of the first tower top discharging pump 104 is divided into two bye-passes, and the tower top section of one of bye-pass and product tower 101 is returned
Head piece connects, another bye-pass is connected to DMM2 rectifying column (not shown).The entrance of first tower reactor discharging pump 105 and product tower
101 bottoms material outlet connection, the outlet of the first tower reactor discharging pump 105 are divided into two bye-passes, one of bye-pass with
The bottom of towe section refluxing opening connection of product tower 101, another bye-pass are connected with the material inlet for the treatment of column 201.
Refer to Fig. 3, refining system 20 include treating column 201, the second reboiler 202, precool equipment 203, tower top by
Flow container 204, the steam jet pump 205, tower top discharging cooler 209 and the tower reactor discharging that are connected with precooling equipment 203 cool down
Device 210.Second reboiler 202 is arranged at the bottom of towe section for the treatment of column 201.The material inlet and product tower 101 at the middle part for the treatment of column 201
Bottoms material outlet connection.The top material outlet for the treatment of column 201 is connected with precooling equipment 203, tower top by flow container 204 successively
Connect.The bottoms material outlet for the treatment of column 201 is divided into two bye-passes, and one of bye-pass is connected by reboiler circulation pump 208
The second reboiler 202 is connected to, another bye-pass is connected to DMM5-8 product storage tanks by the second tower reactor discharging pump 207.Tower top
The second tower top discharging pump 206 is connected with by the outlet of flow container 204.The outlet of second tower top discharging pump 206 is divided into two bye-passes,
One of bye-pass is connected with the tower top section refluxing opening for the treatment of column 201, another bye-pass is connected to impurity removed system 30.Tower top
Discharging cooler 209 is arranged on the bye-pass between the second tower top discharging pump 206 and impurity removed system 30.Tower reactor discharging cooler
210 are arranged on the bye-pass between the second tower reactor discharging pump 207 and DMM5-8 product storage tank (not shown).
Precooling equipment 203 includes the first cooler 211 and the second cooler 212, entrance and the essence of the first cooler 211
The top material outlet connection of tower 201 processed, the outlet of the first cooler 211 is respectively with tower top by 204 and second cooler of flow container
212 entrance connection, the outlet of the second cooler 212 is connected with tower top by the entrance of flow container 204.
Fig. 4 is refer to, impurity removed system 30 includes the first adsorption tanks 301 and the second adsorption tanks 302 in parallel, the first adsorption tanks
301 and second the entrances of adsorption tanks 302 be connected with tower top by the outlet of flow container 204, the first adsorption tanks 301 and the second adsorption tanks
302 outlet is connected with DMM3-4 product storage tanks.
The method for preparing polymethoxy dimethyl ether using above-mentioned polymethoxy dimethyl ether refining spearation system 100, including：
(1) the DMM2-8 products from lightness-removing column are delivered in product tower 101, will be isolated by distillation
DMM2 products are from the output of the top of product tower 101 to DMM2 product storage tanks 103, by isolated DMM3-8 products from product tower
101 bottoms are exported to treating column 201；Wherein, the operation temperature of product tower 101 is 138 DEG C；
(2) by the rectifying in treating column 201 of DMM3-8 products, isolated DMM3-4 products are pushed up from treating column 201
Portion is exported is cooled to 40 DEG C into precooling equipment 203, and isolated DMM5-8 products are exported from 201 bottom for the treatment of column,
DMM5-8 product discharges are divided into two strands, wherein one under the action of the reboiler circulation pump 208 after the utilization of the second reboiler 202
Return again in treating column 201, another strand is disclosed as output of products, dress；Wherein, the operation temperature for the treatment of column 201 is 173
℃；
(3) DMM3-4 products are subjected to removal of impurities processing in impurity removed system 30；Wherein, the running temperature of impurity removed system 30 is not
Higher than 80 DEG C.
Above-mentioned steps (2) include step in detail below：
(21) before start, the pipeline and pump for the treatment of column 201 is preheated, are preheated to 75-80 DEG C；
(22) the cooling water outlet and inlet valve for precooling equipment 203 is opened, opens steam jet pump 205, and adjust essence
Pressure extremely -94KPa in 201 tower of tower processed；
(23) treating column 201 is fed, and establishes bottom of towe liquid level；When bottom of towe liquid level accounts for the 20% of 201 volume for the treatment of column, open
Second reboiler 202, the running temperature for adjusting 201 tower reactor for the treatment of column are 170-175 DEG C, and tower top temperature is 95-100 DEG C；Control
Bottom of towe normal operation liquid level is account for 201 volume for the treatment of column 60%；
(24) the second tower reactor discharging pump 207 is opened when DMM5 contents reach 28% in 201 kettle material for the treatment of column, is produced
DMM5-8 products；The second tower top discharging pump 206 is opened when the DMM3-4 purity of 201 tower top for the treatment of column reaches 99.5%, will
DMM3-4 products are delivered in impurity removed system 30.
The operation principle of the polymethoxy dimethyl ether refining spearation system 100 of the present invention is illustrated below.
DMM2-8 products from lightness-removing column (not shown) are delivered in rough tower and carry out separated, obtain DMM2 productions
Product and DMM3-8 products.Isolated DMM2 is exported into output from the top material of rough tower, in DMM2 product storage tanks 103
Collect.The outlet of DMM2 product storage tanks 103 is connected with the first tower top discharging pump 104, in the effect of the first tower top discharging pump 104
Under, a part of DMM2 products are pumped directly to DMM2 rectifying columns, further purification, and another part is pumped to the top section of rough tower,
Distilled again, improve DMM2 product purities.Isolated DMM3-8 is exported into output from the bottoms material of rough tower,
Under the action of first tower reactor discharging pump 105, a part of DMM3-8 products are pumped directly to treating column 201, carry out next step separation,
Another part is pumped to the bottom section of rough tower, is distilled again, the DMM2 being mingled in DMM3-8 products is separated.
DMM3-8 products from rough tower are inputted from the material inlet for the treatment of column 201, after rectifying, obtain DMM3-4 productions
Product and DMM5-8 products.Isolated DMM3-4 is exported into output from the top material for the treatment of column 201, through cooling device 203
After (the first cooler 211 and the second cooler 212) cooling, collected in tower top in by flow container 204.Tower top is gone out by flow container 204
Mouth is connected with the second tower top discharging pump 206, and under the action of the second tower top discharging pump 206, a part of DMM3-4 products directly pump
Send to tower top discharging cooler 209, further after cooling, be delivered to impurity removed system 30 and carry out removal of impurities processing；Another part pumps
To the top section for the treatment of column 201, rectifying again is carried out, improves DMM3-4 product purities.By isolated DMM5-8 from treating column
201 bottoms material outlet output, and it is divided into two strands, one DMM5-8 product pumps under the action of the second tower reactor discharging pump 207
Send to tower reactor discharging cooler 210, cooled down, then dress is disclosed；Work of another strand of DMM5-8 product in reboiler circulation pump 208
It is pumped under in the second reboiler 202, provides heat source for the second reboiler 202, returned again to after heat exchange into treating column 201,
Rectifying again is carried out, the DMM3-4 being mingled in DMM5-8 products is separated.
First adsorption tanks of the other input value impurity removed system 30 of two stock of DMM3-4 production sharings of autofining in future tower 201
301 and second carry out adsorption-edulcoration in adsorption tanks 302, remove remaining a small amount of formaldehyde in DMM3-4 products, obtain refined DMM3-
4 products.
Comparative example
Existing DMMn products separating technology flow is as follows：
(1) the DMM2-8 products from C-33060 lightness-removing columns enter C-33080 products tower by rectifying by DMM2 and
DMM3-8 is separated, and heat source is heated from tower reactor reboiler steam；DMM2 removes DMM2 product storage tanks from tower top discharging；DMM3-8 is by tower
Kettle discharging is pumped into thin film evaporator.The tower operation temperature is 138 DEG C；
(2) E-33084 thin film evaporators ejection material is DMM3-6, is sent into after the first cooler and the cooling of the second cooler
Product impurity absorption tank, removes a small amount of formaldehyde in product；The discharging of thin film evaporator bottom is heavy component (n is more than 6) dereaction device
The reaction was continued.
Product form made from the technique only has DMM2 and DMM3-6 products, and species is less.
The present invention and existing process are subjected to energy consumption and Cost comparisons, the results are shown in Table 1.
Table 1
As it can be seen from table 1 the present invention, relative to existing process, in addition to product category is more abundant, it is produced into
Originally 50% of existing process or so is also only, has greatly saved production cost.
The foregoing is merely presently preferred embodiments of the present invention, is not intended to limit the invention, it is all the present invention spirit and
Within principle, any modification, equivalent replacement, improvement and so on, should all be included in the protection scope of the present invention.
Claims (9)
- A kind of 1. polymethoxy dimethyl ether refining spearation system, it is characterised in that including：Sequentially connected rough system, refine System and impurity removed system；The rough system includes product tower, the first reboiler and DMM2 product storage tanks；First reboiler is arranged at described The bottom of towe section of product tower, the top material outlet of the product tower are connected with the DMM2 product storage tanks, the bottom of the product tower Portion's material outlet is connected to the refining system by the first tower reactor discharging pump；The refining system includes treating column, the second reboiler, precooling equipment, tower top and is set by flow container and with the precooling The steam jet pump of standby connection；Second reboiler is arranged at the bottom of towe section of the treating column；Thing in the middle part of the treating column Expect that the bottoms material outlet of entrance and the product tower connects, the top material outlet of the treating column successively with the precooling Equipment, the tower top are connected by flow container, and the bottoms material outlet of the treating column is divided into two bye-passes, one of bye-pass Second reboiler is connected to by reboiler circulation pump, another bye-pass is connected to by the second tower reactor discharging pump DMM5-8 product storage tanks；The tower top is connected with the second tower top discharging pump by the outlet of flow container, the second tower top discharging pump Outlet is divided into two bye-passes, and one of bye-pass is connected with the tower top section refluxing opening of the treating column, another bye-pass It is connected to the impurity removed system.
- 2. polymethoxy dimethyl ether refining spearation system according to claim 1, it is characterised in that the precooling equipment Including the first cooler and the second cooler, the entrance of first cooler connects with the top material outlet of the treating column Connecing, the outlet of first cooler is connected with the tower top by the entrance of flow container and second cooler respectively, and described The outlet of two coolers is connected with the tower top by the entrance of flow container.
- 3. polymethoxy dimethyl ether refining spearation system according to claim 2, it is characterised in that the refining system is also Discharge cooler including tower top, tower top discharging cooler be arranged at the second tower top discharging pump and the impurity removed system it Between bye-pass on.
- 4. polymethoxy dimethyl ether refining spearation system according to claim 3, it is characterised in that the refining system is also Including tower reactor discharging cooler, the tower reactor discharging cooler is arranged at the second tower reactor discharging pump and the DMM5-8 products On bye-pass between storage tank.
- 5. polymethoxy dimethyl ether refining spearation system according to claim 1, it is characterised in that first tower reactor goes out Expect that the entrance of pump is connected with the bottoms material outlet of the product tower, the outlet of the first tower reactor discharging pump is divided into two branch pipes Road, one of bye-pass are connected with the bottom of towe section refluxing opening of the product tower, the thing of another bye-pass and the treating column Expect entrance connection.
- 6. according to claim 1-5 any one of them polymethoxy dimethyl ether refining spearation systems, it is characterised in that described thick System processed further includes the first tower top discharging pump, and the entrance of the first tower top discharging pump and the material of the DMM2 product storage tanks go out Mouth connection, the outlet of the first tower top discharging pump are divided into two bye-passes, the tower of one of bye-pass and the product tower The connection of section refluxing opening is pushed up, another bye-pass is connected to DMM2 rectifying columns.
- 7. polymethoxy dimethyl ether refining spearation system according to claim 1, it is characterised in that the impurity removed system bag Include the first adsorption tanks and the second adsorption tanks of parallel connection, the entrances of first adsorption tanks and second adsorption tanks with the institute Tower top is stated to be connected by the outlet of flow container, the outlets of first adsorption tanks and second adsorption tanks with DMM3-4 product storage tanks Connection.
- 8. prepare polymethoxy dimethyl ether using claim 1-7 any one of them polymethoxy dimethyl ether refining spearation systems Method, it is characterised in that including：(1) the DMM2-8 products from lightness-removing column are delivered in product tower, by distillation, by isolated DMM2 products from Product top of tower is exported to DMM2 product storage tanks, and isolated DMM3-8 products are exported to treating column from product tower bottom； Wherein, the operation temperature of product tower is 138 DEG C；(2) rectifying in treating column by DMM3-8 products, isolated DMM3-4 products are exported to pre- at the top for the treatment of column 40 DEG C are cooled in cooling device, isolated DMM5-8 products are exported from refined tower bottom, DMM5-8 product discharges point Into two strands, wherein one returns again to treating column under the action of reboiler circulation pump after second reboiler utilization In, another strand is disclosed as output of products, dress；Wherein, the operation temperature for the treatment of column is 173 DEG C；(3) DMM3-4 products are subjected to removal of impurities processing in impurity removed system；Wherein, the running temperature of impurity removed system is not higher than 80 ℃。
- 9. according to the method described in claim 8, it is characterized in that, step (2) includes step in detail below：(21) before start, the pipeline and pump for the treatment of column is preheated, are preheated to 75-80 DEG C；(22) the cooling water outlet and inlet valve for precooling equipment is opened, opens steam jet pump, and adjust in treating column tower Pressure extremely -94KPa；(23) treating column is fed, and establishes bottom of towe liquid level；When bottom of towe liquid level accounts for the 20% for the treatment of column volume, open second and boil again Device, the running temperature for adjusting treating column tower reactor are 170-175 DEG C, and tower top temperature is 95-100 DEG C；Control tower bottom normal operation liquid Position is to account for the 60% for the treatment of column volume；(24) the second tower reactor discharging pump, extraction DMM5-8 productions are opened when DMM5 contents reach 28% in treating column kettle material Product；The second tower top discharging pump is opened when the DMM3-4 purity of refined column overhead reaches 99.5%, DMM3-4 products are delivered to In impurity removed system.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113087602A (en) * | 2020-01-09 | 2021-07-09 | 中国石油化工股份有限公司 | Production and refining method of polymethoxy dimethyl ether |
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| Publication number | Priority date | Publication date | Assignee | Title |
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