CN202164251U - Residual heat recycling device for aldehyde steam of furfuraldehyde - Google Patents
Residual heat recycling device for aldehyde steam of furfuraldehyde Download PDFInfo
- Publication number
- CN202164251U CN202164251U CN2011202925418U CN201120292541U CN202164251U CN 202164251 U CN202164251 U CN 202164251U CN 2011202925418 U CN2011202925418 U CN 2011202925418U CN 201120292541 U CN201120292541 U CN 201120292541U CN 202164251 U CN202164251 U CN 202164251U
- Authority
- CN
- China
- Prior art keywords
- communicated
- aldehyde
- steam
- heat boiler
- waste heat
- 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.)
- Expired - Lifetime
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a residual heat recycling device for aldehyde steam of furfuraldehyde. The residual heat recycling device comprises an aldehyde steam buffer tank, a stock solution trough, a primary tower, a phase splitter, a condenser I, a condenser II, a gross aldehyde refining device, and an exhaust heat boiler which are communicated with a hydrolytic kettle pipeline, wherein the tube pass of the exhaust heat boiler is communicated with the aldehyde steam buffer tank; the other end of the tube pass of the exhaust heat boiler is communicated with the stock solution trough and a separator; the bottom of the separator is communicated with the middle of the stock solution trough; the bottom of the stock solution trough is communicated with the primary tower; the top of the primary tower is communicated with that of the phase splitter; the condenser II is arranged on a pipeline; and the middle upper part of the phase splitter is communicated with the middle of the primary tower. Through the adoption of the residual heat recycling device, each ton of aldehyde steam containing 8 percent of aldehyde can produce 0.633 ton of 0.4MPa steam and save 35.217 ton of circulating water; equivalently, each ton of refined aldehyde produces 8.28 ton of low pressure steam, and saves 60.688 ton of circulating water; and the steam consumption of each ton of furfuraldehyde is reduced from 20-22 tons to 12-14 tons.
Description
Technical field
The utility model relates to heat recovery and utilization field in the industrial production, particularly a kind of furfural aldehyde vapour residual heat recovery device.
Background technology
Furfural is claimed furtural again, and molecular formula is C
5H
4O
2, relative molecular weight 96.8, normal temperature are the colourless or light yellow liquid that the almond flavor is arranged down.Be widely used in medicine, agricultural chemicals, synthetic resins, synthon, viton etc.Make with the agricultural byproducts hydrolysis that contains piperylene in the industry, promptly piperylene at first is hydrolyzed into pentose, and pentose closed loop dehydration again generates furfural.
Domestic furfural production mostly is to be raw material with the corn cob, and above-mentioned two-step reaction is carried out in a reactor drum (hydrolysis kettle) simultaneously, is commonly called as " single stage method ".The hydrolysis kettle volume is 10～15m
3The vertical retort of liner acid-proof cement, gap operating.Furfural dregs produces steam as boiler oil and supplies water and separate and distill refining plant and use.One ton of furfural of every production consumes 12～15 tons of corn cobs approximately, 20-22 ton steam, and 250～300 kilograms of sulfuric acid produce 12～15 tons of furfural dregs.
Aldehyde vapour condensation process flow is in the most general " single stage method " furfural production technology of present domestic use: from the high temperature aldehyde vapour (150-170 ℃) of hydrolysis kettle earlier through aldehyde vapour surge tank; Again through the heat exchange of fore-running Tata still; Aldehyde stripping temperature after the heat exchange is about 150 ℃; 150 ℃ aldehyde vapour is the stoste below 97.8 ℃ (azeotropic points of furfural and water) through aldehyde vapour condenser condenses, specifically installs schema and sees accompanying drawing 1.
Aldehyde vapour becomes liquid state by gaseous state in the aldehyde vapour condensation process, emits a large amount of latent heat, therefore needs to consume a large amount of recirculated cooling waters, has great heat energy utilization space.
Summary of the invention
In order to overcome the above problems, the utility model provides a kind of furfural aldehyde vapour residual heat recovery device that makes full use of aldehyde vapour heat, economized cycle water coolant and heat.
The utility model is realized in the following manner:
A kind of furfural aldehyde vapour residual heat recovery device comprises the aldehyde vapour surge tank that is communicated with the hydrolysis kettle pipeline, former liquid bath, primary tower, phase splitter, condensing surface I, condensing surface II, hair aldehyde refining plant, also comprises waste heat boiler; The tube side of waste heat boiler is communicated with aldehyde vapour surge tank pipeline, and the other end top of waste heat boiler tube side is communicated with former liquid bath top duct, and pipeline is provided with the condensing surface I; The other end bottom of waste heat boiler tube side is communicated with the separator middle and upper part; The separator bottom is communicated with former liquid bath central tube road, and the stoste trench bottom is communicated with primary tower middle part pipeline, and the primary tower top is communicated with the phase splitter top duct; And pipeline is provided with the condensing surface II; The phase splitter middle and upper part is communicated with primary tower middle part pipeline, and the phase splitter bottom is communicated to a mao aldehyde refining plant, and the primary tower bottom is communicated to wastewater disposal basin.
The shell side import of waste heat boiler is a soft water, exports to be LP steam, and the shell side outlet of waste heat boiler is communicated to the steam using appts.
The steam using appts is stoste water distilling apparatus or hair aldehyde refining plant.
The separator top is communicated with the other end top duct of waste heat boiler tube side.
The beneficial effect of the utility model:
Adopt this furfural aldehyde vapour residual heat recovery device; The aldehyde vapour that contains aldehyde 8% per ton can produce 0.633 ton of 0.4MPa steam, and 35.217 tons in economized cycle water is amounted to smart aldehyde per ton and produced 8.28 tons of LP steams; Save 60.688 tons of recirculated waters, the steam consumption of furfural per ton can be reduced to the 12-14 ton by the 20-22 ton.
Description of drawings
Accompanying drawing 1 is traditional aldehyde vapour condensing works synoptic diagram,
Accompanying drawing 2 is the utility model furfural aldehyde vapour residual heat recovery device synoptic diagram,
Among the figure, 1, aldehyde vapour, 2, aldehyde vapour surge tank, 3, waste heat boiler, 4, soft water; 5, LP steam, 6, separator, 7, former liquid bath, 8, primary tower, 9, phase splitter; 10, condensing surface I, 11, the condensing surface II, 12, hair aldehyde refining plant, 13, wastewater disposal basin, 14, the steam using appts.
Embodiment
Can smooth and easyly flow to the liquid in the pipeline of separator 6 for the other end bottom that makes waste heat boiler 3 tube sides, separator 6 tops are communicated with the other end top of waste heat boiler 3 tube sides.
In line with the thought of energy-saving and emission-reduction and cleaner production, the utility model is creationary to be applied to the aldehyde vapour condensation operation that furfural is produced with waste heat boiler 3, can successfully realize the comprehensive utilization of aldehyde vapour waste heat.Whole process flow is following:
Behind aldehyde vapour surge tank 2, get into waste heat boiler 3 from the temperature of hydrolysis kettle at 150-170 ℃ high temperature aldehyde vapour 1; Aldehyde vapour is walked tube side; The steam condenses of soft water 4 or other operations is walked shell side; High temperature aldehyde vapour 1 is accomplished heat exchange through heat exchanging pipe with soft water 4 in waste heat boiler, soft water 4 is heated to form the LP steam 5 of 0.3-0.4MPa and draws from waste heat boiler 3 shell side tops; The stoste that most of aldehyde vapour 1 condenses into below 97.8 ℃ is drawn from waste heat boiler 3 tube sides bottom, gets into former liquid/gas separator 6, gets into former liquid bath 7 then; In waste heat boiler 3 tube sides few part not agglomerative aldehyde vapour get rid of from waste heat boiler 3 tube side tops; Be condensed into stoste through condensing surface I 10 again, get into former liquid bath 7, stoste gets into primary tower 8 and carries out fore-running from former liquid bath 7 bottoms; Distilled gas comes out to be condensed into liquid through condensing surface II 11 from cat head and gets into phase splitter 9; Through phase-splitting, the liquid hair aldehyde of lower floor gets into a hair aldehyde refining plant 12 and makes with extra care, and the water that a small amount of furfural is contained on the upper strata gets into primary tower 8 again and distills.The liquid of primary tower 8 bottoms is waste water at the bottom of the tower, and its composition: organic acid is about 2%, and furfural is about 0.1%, and all the other major parts are water.Waste water advances wastewater disposal basin at the bottom of the tower.
The pressure of soft water 4 liquid levels in the waste heat boiler 3, the pressure of LP steam 5 and waste heat boiler 3 aldehyde vapor outlets is suitably adjusted according to steam production with the vapour needs through automatic regulating valve control.
Adopt this furfural aldehyde vapour residual heat recovery device, the steam consumption of furfural per ton can be reduced to the 12-14 ton by the 20-22 ton, and calculation of correlation is following:
Every 1000kg aldehyde vapour heat that (165 ℃ contain aldehyde 8%), total condensation discharged:
Q
H=W
Water* r
Water+ W
Aldehyde* r
Aldehyde=920kg * 2071.5kj/kg+80kg * 504kj/kg=1.946 * 10
6Kj
Every 1000kg water of condensation (about 100 ℃) is heated to form 0.4MPa steam (about 152 ℃) institute's heat requirement:
Q
C=W
Water* (H
152 ℃ of vapour-H
100 ℃ in water)=1000kg * (2752.8kj/kg-416.9kj/kg)=2.336 * 10
6Kj
Aldehyde vapour as 80% is condensed in useless pot, 5% thermosteresis wherein, and aldehyde vapour then per ton liberated heat during through waste heat boiler:
Q
Put=Q
H* 80% * 95%=1.946 * 10
6* 80% * 95%=1.479 * 10
6Kj
If with this part heat of recirculated water heat exchange, the amount of required recirculated water is:
W
Water=Q
Put/ (Cp* △ t)=1.479 * 10
6Kj/ (4.2kj/kg ℃ * 10 ℃)=35.217 tons
Can be got by above calculating: aldehyde vapour per ton (containing aldehyde 8%) can produce 0.633 ton of 0.4MPa steam, 35.217 tons in economized cycle water.Amount to smart aldehyde per ton and produce 8.28 tons of LP steams, save 60.688 tons of recirculated waters (content of furfural is 90% in the hair aldehyde, and hair aldehyde calculates by 86% to the recovery of smart aldehyde).
Claims (4)
1. a furfural aldehyde vapour residual heat recovery device comprises the aldehyde vapour surge tank that is communicated with the hydrolysis kettle pipeline, former liquid bath, primary tower, phase splitter, condensing surface I, condensing surface II, hair aldehyde refining plant, it is characterized in that also comprising waste heat boiler; The tube side of waste heat boiler is communicated with aldehyde vapour surge tank pipeline, and the other end top of waste heat boiler tube side is communicated with former liquid bath top duct, and pipeline is provided with the condensing surface I; The other end bottom of waste heat boiler tube side is communicated with the separator middle and upper part; The separator bottom is communicated with former liquid bath central tube road, and the stoste trench bottom is communicated with primary tower middle part pipeline, and the primary tower top is communicated with the phase splitter top duct; And pipeline is provided with the condensing surface II; The phase splitter middle and upper part is communicated with primary tower middle part pipeline, and the phase splitter bottom is communicated to a mao aldehyde refining plant, and the primary tower bottom is communicated to wastewater disposal basin.
2. furfural aldehyde vapour residual heat recovery device according to claim 1 is characterized in that the shell side import of waste heat boiler is a soft water, exports to be LP steam, and the shell side outlet of waste heat boiler is communicated to the steam using appts.
3. furfural aldehyde vapour residual heat recovery device according to claim 2 is characterized in that the steam using appts is stoste water distilling apparatus or hair aldehyde refining plant.
4. furfural aldehyde vapour residual heat recovery device according to claim 1 is characterized in that the separator top is communicated with the other end top duct of waste heat boiler tube side.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202925418U CN202164251U (en) | 2011-08-12 | 2011-08-12 | Residual heat recycling device for aldehyde steam of furfuraldehyde |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011202925418U CN202164251U (en) | 2011-08-12 | 2011-08-12 | Residual heat recycling device for aldehyde steam of furfuraldehyde |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202164251U true CN202164251U (en) | 2012-03-14 |
Family
ID=45800091
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011202925418U Expired - Lifetime CN202164251U (en) | 2011-08-12 | 2011-08-12 | Residual heat recycling device for aldehyde steam of furfuraldehyde |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202164251U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103551362A (en) * | 2013-10-31 | 2014-02-05 | 宏业生化股份有限公司 | Novel process for comprehensively utilizing agricultural wastes |
| CN103822456A (en) * | 2014-02-26 | 2014-05-28 | 邢台市大曹庄管理区康丰化工有限公司 | Waste heat collection device for furfural production |
| CN108926862A (en) * | 2018-09-29 | 2018-12-04 | 天津中福环保科技股份有限公司 | Light naphtha recyclable device, its skid structure and light naphtha recovery method in a kind of dangerous waste process field |
| CN109724440A (en) * | 2018-12-10 | 2019-05-07 | 安徽金禾实业股份有限公司 | Total energy approach method and device in furfural production |
-
2011
- 2011-08-12 CN CN2011202925418U patent/CN202164251U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103551362A (en) * | 2013-10-31 | 2014-02-05 | 宏业生化股份有限公司 | Novel process for comprehensively utilizing agricultural wastes |
| CN103551362B (en) * | 2013-10-31 | 2015-10-21 | 宏业生化股份有限公司 | Agricultural wastes comprehensive utilization new technology |
| CN103822456A (en) * | 2014-02-26 | 2014-05-28 | 邢台市大曹庄管理区康丰化工有限公司 | Waste heat collection device for furfural production |
| CN108926862A (en) * | 2018-09-29 | 2018-12-04 | 天津中福环保科技股份有限公司 | Light naphtha recyclable device, its skid structure and light naphtha recovery method in a kind of dangerous waste process field |
| CN108926862B (en) * | 2018-09-29 | 2024-03-22 | 天津中福环保科技股份有限公司 | Light solvent recovery device in hazardous waste treatment field, skid-mounted structure thereof and light solvent recovery method |
| CN109724440A (en) * | 2018-12-10 | 2019-05-07 | 安徽金禾实业股份有限公司 | Total energy approach method and device in furfural production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101130530B (en) | System and method for producing furol by using agricultural and forestry castoff | |
| CN102286544B (en) | A kind of clean preparation method of starch base alcohol fuel | |
| CN106699808B (en) | A kind of acidolysis of producing glyphosate by using glycine and solvent recovery process and device | |
| CN100453137C (en) | Alcohol quinque-towel differential pressure distilling arrangement and technique thereof | |
| CN202164251U (en) | Residual heat recycling device for aldehyde steam of furfuraldehyde | |
| CN106929162B (en) | Acid reducing process for producing glycerol by using waste oil | |
| CN104986910A (en) | Mechanical steam recompression falling film evaporation process method and system | |
| CN106928026B (en) | Method for distilling cellulosic ethanol | |
| CN104387346B (en) | Prepared the method for furfural by pentose multiple stage continuous adverse current reaction, extraction | |
| CN104130224B (en) | The tower continuous treater of furfural production six and furfural treatment technique thereof | |
| CN104151136B (en) | The processing method of butanols-N-BUTYL ACETATE is reclaimed from antibiotic production wastewater | |
| CN103736384A (en) | Treatment process of glyphosate hydrolyzing tail gas | |
| CN106674273B (en) | A kind of hydrolysis device of producing glyphosate by using glycine | |
| CN110128379A (en) | A kind of method that serialization prepares furfural | |
| CN203307083U (en) | Negative pressure ammonia distiller by using raw gas waste heat as heat source | |
| CN102161903B (en) | Coal tar alkali-free short-flow normal/reduced-pressure distillation process and device | |
| CN204824504U (en) | Machinery vapor recompression falling film evaporation process systems | |
| CN101108838B (en) | System and method of manufacturing furol with pentose solution | |
| CN106929163B (en) | Acid reducing system for waste oil | |
| CN105217654B (en) | Alkylation waste sulfuric acid recycling treatment device and method | |
| CN210620240U (en) | Improve analytic system of hydrochloric acid of thermal efficiency | |
| CN210096970U (en) | Furfural multiple-effect reaction rectifying device | |
| CN106467457B (en) | Method for continuously producing 5-chloro-2-pentanone | |
| CN112409174A (en) | Preparation device and method of 3, 3-methyl dimethacrylate | |
| CN205556518U (en) | Economizer of refined system of acetonitrile |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20120314 |