CN205953886U - Take dimethyl ether production system of cogeneration - Google Patents
Take dimethyl ether production system of cogeneration Download PDFInfo
- Publication number
- CN205953886U CN205953886U CN201620804557.5U CN201620804557U CN205953886U CN 205953886 U CN205953886 U CN 205953886U CN 201620804557 U CN201620804557 U CN 201620804557U CN 205953886 U CN205953886 U CN 205953886U
- Authority
- CN
- China
- Prior art keywords
- methanol
- dimethyl ether
- methyl alcohol
- reboiler
- distillation column
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a take dimethyl ether production system of cogeneration, synthesize the pre -heater including methyl alcohol, methyl alcohol is synthesized the pre -heater top and is connected with methyl alcohol vaporization tower upper portion, methyl alcohol vaporization top of the tower portion and heat exchanger sub -unit connection, heat exchanger upper portion is connected with the reactor top, the reactor bottom is connected bottom the heat exchanger, the heat exchanger top is connected with the upper portion that the pre -heater is synthesized to methyl alcohol, the upper portion of pre -heater and the sub -unit connection of dimethyl ether rectifying column are synthesized to methyl alcohol, the dimethyl ether rectifying column is connected with the dimethyl ether holding tank, the bottom and the upper portion of methyl alcohol recovery tower of dimethyl ether rectifying column are connected, being connected of pre -heater is synthesized with methyl alcohol to the methyl alcohol recovery tower, the bottom and the methyl alcohol of methyl alcohol recovery tower are synthesized the pre -heater and are connected, methyl alcohol recovery tower lower part is equipped with methyl alcohol recovery tower reboiler, reactor upper portion is connected with the steam gas bag, and the steam gas bag is connected with back pressure turbine, and back pressure turbine is connected with methyl alcohol recovery tower reboiler. The utility model discloses the energy realizes that cascade utilization takes cogeneration, and the energy consumption is low.
Description
Technical field
This utility model belongs to chemical products production equipment field and in particular to a kind of dimethyl ether with cogeneration produces
System.
Background technology
Dimethyl ether, also known as methyl ether, is important industrial chemicals, due to its good compressible, condensation, vaporizing property, wide
General apply in fields such as industry, agricultural, medical treatment, daily life, dimethyl ether future be additionally operable to replace vehicle fuel, L. P. G
Gas, town gas etc., market prospect is extremely wide, due to petroleum resources shortage, rich coal resources and people's environmental consciousness
Strengthen, dimethyl ether is obtained by methanol dehydration, be increasingly subject to as the clean fuel changing into from coal pay attention to, become state in recent years
The inside and outside product competitively developed and produce, is the industry that home and abroad is first developed.Produce the method that dimethyl ether is adopted at present,
Most of is two step method, and China or even the world all adopt high temperature catalyst to react, and reaction conversion ratio is low, only 80-85%, and
In terms of energy utilization, efficiency is low, and only 50%, so producing dimethyl ether, mainly outer heat supply can be manufacturing, and energy consumption is big, becomes
It is difficult to effective popularization and application, dimethyl ether produces and also much can not meet the needs that modernization industry produces this height.
Utility model content
For problems of the prior art, this utility model provides a kind of dimethyl ether with cogeneration to produce system
System, can produce that conversion per pass is low by effectively solving dimethyl ether, energy consumption is big, the problem of high cost.
For solving above-mentioned technical problem, this utility model employs the following technical solutions：
A kind of dimethyl ether production system with cogeneration, including methanol synthesis preheater, described methanol synthesis preheater
Top is connected with methyl alcohol vaporizing tower top, and methyl alcohol vaporizing top of tower is connected with heat exchanger bottom, heat exchanger top and reactor top
Portion connects, and reactor bottom is connected with exchanger base, and heat exchanger top is passed through pipeline I and connected with the top of methanol synthesis preheater
Connect, the top of methanol synthesis preheater is connected with the bottom of dimethyl ether rectifying column by pipeline II, the top of dimethyl ether rectifying column
It is connected with dimethyl ether holding tank via dimethyl ether rectifying column water cooler, the bottom of dimethyl ether rectifying column and the top of methanol distillation column
Connect, the top of methanol distillation column is connected with the methanol feed line of methanol synthesis preheater via methanol distillation column water cooler,
The bottom of methanol distillation column is connected with methanol synthesis preheater, and the bottom of described methanol distillation column is provided with methanol distillation column and boils
Device；Described reactor top is connected with steam gas bag, and steam gas bag is connected with back pressure turbine, back pressure turbine and Methanol Recovery
Tower reboiler connects.
Described methanol gasifying tower bottom is provided with Steam reboiler and waste heat reboiler, and Steam reboiler is with methanol gasifying tower even
Logical, waste heat reboiler connects with methanol gasifying tower.
One of charging aperture of described waste heat reboiler is connected with exchanger base, and one of them of waste heat reboiler goes out
Material mouth is connected with pipeline I.
Described methanol distillation column Steam reboiler is connected with methanol distillation column, and methanol distillation column Steam reboiler and pipe
Road II is connected.
The beneficial effects of the utility model：This utility model carries the producing dimethyl ether by dehydrating methanol system of cogeneration composition
System, thick diformazan ether mixture without condensation, is directly entered dimethyl ether rectifying column, carries out dimethyl ether rectification using reaction heat, and
And mixture replaces outer heating load for methanol reaction heat in heating evaporation tower after reacting, methanol conversion is high, product quality
Height, energy realizes cascade utilization band cogeneration function, and capacity usage ratio is high（Energy consumption is low）, realize energy-conservation, reduce production cost
Purpose, make full use of resource, using energy, reach total energy approach, have advanced, safe efficient, energy-conservation, small investment,
Low cost, quality are good, non-environmental-pollution（Environmental protection）Distinguishing feature, through repeatedly many batches（10 times）Different amounts of（100-500kg）
Compared with testing and producing dimethyl ether with other methods, this utility model can reduce production cost more than 40%, and capacity usage ratio reaches
More than 80%, methanol conversion per pass improves more than 10%, and does not have environmental pollution, and its economic and social benefit is huge, promotes
Have a extensive future.
Brief description
Fig. 1 is structural representation of the present utility model.
Specific embodiment
With reference to specific embodiment, this utility model is described further.It should be understood that following examples are only used for
, not for limiting scope of the present utility model, the person skilled in the art in this field can be according to above-mentioned practicality for bright this utility model
New content is made some nonessential improvement and is adjusted.
As shown in figure 1, a kind of dimethyl ether production system with cogeneration, including methanol synthesis preheater 1, described methanol
Comprehensive preheater 1 top is connected with methyl alcohol vaporizing tower 2 top, and methanol gasifying tower 2 bottom is provided with Steam reboiler 8 and waste heat boils again
Device 9, Steam reboiler 8 is connected with methanol gasifying tower 2, and waste heat reboiler 9 connects with methanol gasifying tower 2；
Methyl alcohol vaporizing tower 2 top is connected with heat exchanger 3 bottom, and heat exchanger 3 top is connected with reactor 4 top, reactor 4
Bottom is connected with heat exchanger 3 bottom, and heat exchanger 3 top is passed through pipeline I 06 and is connected with the top of methanol synthesis preheater 1, methanol
The top of comprehensive preheater 1 is connected with the bottom of dimethyl ether rectifying column 6 by pipeline II 07, the top warp of dimethyl ether rectifying column 6
It is connected with dimethyl ether holding tank 14 by dimethyl ether rectifying column water cooler 12；One of charging aperture of described waste heat reboiler 9 with
Heat exchanger 3 bottom connects, and one of discharging opening of waste heat reboiler 9 is connected with pipeline I 06；
The bottom of dimethyl ether rectifying column 6 is connected with the top of methanol distillation column 5, and the top of methanol distillation column 5 is via methanol
Recovery tower water cooler 11 is connected with the methanol feed line 01 of methanol synthesis preheater 1, and the bottom of methanol distillation column 5 is comprehensive with methanol
Close preheater 1 to connect, the bottom of described methanol distillation column 5 is provided with methanol distillation column reboiler 10；Methanol distillation column steam boils again
Device 10 is connected with methanol distillation column 5, and methanol distillation column Steam reboiler 10 is connected with pipeline II 07；Described reactor 4
Top is connected with steam gas bag 13, and steam gas bag 13 is connected with back pressure turbine 7, and back pressure turbine 7 and methanol distillation column boil again
Device 10 connects.
Work process of the present utility model is as follows：Methanol entrance methanol synthesis preheater 1 is preheating to 90 DEG C about and enters methanol
Vaporization tower 2, in 130 DEG C -135 DEG C entrance heat exchangers 3 after methyl alcohol vaporizing, heat exchange to 220 DEG C about enter reactor 4, methanol warp
Cross under modified acidic group middle temperature catalyst catalysis, after 240--300 DEG C of dehydration, enter heat exchanger 3, enter methanol after cooling comprehensive
Close preheater 1, then cool to 130 DEG C about, send into dimethyl ether rectifying column 6, after rectification, pass through water cooler 12, diformazan ether product send
Enter storage tank 14, through the residual liquid after rectifying column 6 rectification, return to methanol distillation column 5, reclaim remaining a small amount of methanol, recycle.
Cogeneration flow process：20 DEG C of soft water are sent into reactor 4 via soft water pipeline 012, the energy released through reactor 4
Amount is heated, produce about 4.0MPa about steam send into steam drum 13, steam goes out drum 13 and enters back into back pressure electromotor
7, steam back pressure to 1.3MPa about, it is re-fed into methanol distillation column reboiler 10.
Of the present utility model ultimate principle and principal character and of the present utility model advantage have been shown and described above.This
The technical staff of industry, it should be appreciated that this utility model is not restricted to the described embodiments, retouches in above-described embodiment and description
That states simply illustrates principle of the present utility model, on the premise of without departing from this utility model spirit and scope, this utility model
Also have various changes and modifications, these changes and improvements both fall within the range of claimed this utility model.This practicality is new
Type claims scope by appending claims and its equivalent thereof.
Claims (4)
1. a kind of dimethyl ether production system with cogeneration, including methanol synthesis preheater（1）It is characterised in that：Described first
Alcohol synthesis preheater（1）Top and methyl alcohol vaporizing tower（2）Top connects, methyl alcohol vaporizing tower（2）Top and heat exchanger（3）Bottom is even
Connect, heat exchanger（3）Top and reactor（4）Top connects, reactor（4）Bottom and heat exchanger（3）Bottom connects, heat exchanger
（3）Pipeline I is passed through at top（06）With methanol synthesis preheater（1）Top connect, methanol synthesis preheater（1）Top pass through
Pipeline II（07）With dimethyl ether rectifying column（6）Bottom connect, dimethyl ether rectifying column（6）Top via dimethyl ether rectifying column water
Cooler（12）With dimethyl ether holding tank（14）Connect, dimethyl ether rectifying column（6）Bottom and methanol distillation column（5）Top even
Connect, methanol distillation column（5）Top via methanol distillation column water cooler（11）With methanol synthesis preheater（1）Methanol feed pipe
Line（01）Connect, methanol distillation column（5）Bottom and methanol synthesis preheater（1）Connect, described methanol distillation column（5）Bottom
It is provided with methanol distillation column reboiler（10）；Described reactor（4）Top and steam gas bag（13）Connect, steam gas bag（13）With the back of the body
Hydraulic motor（7）Connect, back pressure turbine（7）With methanol distillation column reboiler（10）Connect.
2. the dimethyl ether production system with cogeneration according to claim 1 it is characterised in that：Described methanol gasifying tower
（2）Bottom is provided with Steam reboiler（8）With waste heat reboiler（9）, Steam reboiler（8）With methanol gasifying tower（2）Connection, waste heat
Reboiler（9）With methanol gasifying tower（2）Connection.
3. the dimethyl ether production system with cogeneration according to claim 2 it is characterised in that：Described waste heat reboiler
（9）One of charging aperture and heat exchanger（3）Bottom connects, waste heat reboiler（9）One of discharging opening and pipeline I
（06）Connection.
4. the dimethyl ether production system with cogeneration according to claim 1 it is characterised in that：Described methanol distillation column
Steam reboiler（10）With methanol distillation column（5）It is connected, and methanol distillation column Steam reboiler（10）With pipeline II（07）Phase
Connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620804557.5U CN205953886U (en) | 2016-07-28 | 2016-07-28 | Take dimethyl ether production system of cogeneration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620804557.5U CN205953886U (en) | 2016-07-28 | 2016-07-28 | Take dimethyl ether production system of cogeneration |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205953886U true CN205953886U (en) | 2017-02-15 |
Family
ID=57972484
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620804557.5U Active CN205953886U (en) | 2016-07-28 | 2016-07-28 | Take dimethyl ether production system of cogeneration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205953886U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112142559A (en) * | 2020-09-22 | 2020-12-29 | 吕永华 | Waste heat recovery device for methanol production |
-
2016
- 2016-07-28 CN CN201620804557.5U patent/CN205953886U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112142559A (en) * | 2020-09-22 | 2020-12-29 | 吕永华 | Waste heat recovery device for methanol production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN206695411U (en) | A kind of solar energy high temperature storage and release system based on thermochemical method | |
| CN108546243A (en) | A kind of lithium battery production double tower NMP recycling purification systems and its recycling method of purification | |
| CN201670845U (en) | High temperature solid slag sensible heat recovery device | |
| CN103773315B (en) | A kind of Hydrocarbon phase change heat storage and take natural acid as the preparation method of raw material | |
| CN101274881A (en) | Energy-saving method for producing dimethy ether by boiler with residual heat | |
| CN205953886U (en) | Take dimethyl ether production system of cogeneration | |
| CN101705106A (en) | New energy-saving process for preparing MTG (or DME) with rough (refined) methanol | |
| CN204661587U (en) | A kind of energy-saving carbamide production system | |
| CN203768274U (en) | System for one-time production of gamma-butyrolactone through dehydrogenation and catalytic distillation of 1,4-butanediol | |
| CN105779048B (en) | A kind of low temperature produces the methanation process of synthetic natural gas | |
| CN209024426U (en) | A kind of material liquid preheating device in synthetic methylamine technique | |
| CN106045824B (en) | A kind of dimethyl ether production system and production technology with cogeneration | |
| CN205035295U (en) | Methanol synthesis reaction gas is used for methyl alcohol pre -rectifying tower heating system | |
| CN202595004U (en) | Low energy consumption preparation process system of dimethyl ether | |
| CN206862149U (en) | A kind of waste heat recovery recycling device | |
| CN206219334U (en) | A kind of semi-coke wastewater pretreatment system | |
| CN101851152A (en) | Method for preparing dimethyl ether by methyl alcohol gaseous phase dehydration | |
| CN206001438U (en) | Synthetic ammonia installation residual neat recovering system | |
| CN205740938U (en) | A kind of lubricating oil distillation refining system | |
| CN105777469A (en) | Heat exchanging system and method and use of mixed C4 separation and butene-1 rectification system | |
| CN1166610C (en) | Diglycol material for preparing morpholine | |
| CN204569785U (en) | A kind of device reclaiming DMSO from the DMSO aqueous solution | |
| CN220176830U (en) | Steam energy consumption reducing device of methyl ethyl carbonate device | |
| CN202595005U (en) | Optimized energy-saving dimethyl ether production device | |
| CN202470522U (en) | Carbon dioxide humidifying low temperature waste heat recycling device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |