CN108069828A - A kind of production biodiesel byproduct crude glycerin high-purity purification technique - Google Patents
A kind of production biodiesel byproduct crude glycerin high-purity purification technique Download PDFInfo
- Publication number
- CN108069828A CN108069828A CN201810016944.6A CN201810016944A CN108069828A CN 108069828 A CN108069828 A CN 108069828A CN 201810016944 A CN201810016944 A CN 201810016944A CN 108069828 A CN108069828 A CN 108069828A
- Authority
- CN
- China
- Prior art keywords
- tower
- glycerine
- purity
- steam
- temperature
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- 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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
-
- 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
- B01D3/42—Regulation; Control
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Abstract
The invention discloses a kind of production biodiesel byproduct crude glycerin high-purity purification techniques mainly to include：Pre-distillation goes water removal and light component；Rectifying produces high purity extractive glycerine, higher boiling heavy constituent desalination dedoping step.Pre-distillation column removes the relatively low light component of boiling point, has prevented light component impurity and glycerine is mixed into distillation process.The impurity such as the relatively high high-boiling components of boiling point and salinity are eliminated by destilling tower, high-boiling components is avoided and is mixed into glycerin vapor, since destilling tower tower body is at 16 meters or more, packing layer is up to 8 meters, it is ensured that the high-purity of gained glycerine.By removing salt cellar, the salinity in the organic matters such as high-boiling components stearic acid is eliminated, the organic matters such as stearic acid and salinity is made all to be utilized.Most significant feature is present invention employs new TQK robot control system(RCS)s, realizes being precisely controlled for temperature and flow, it is ensured that glycerine purity reaches more than 99.5%.
Description
Technical field
The present invention relates to the purifications of Organic chemical products, and it is high to be directly related to a kind of production biodiesel byproduct crude glycerin
Purity purifying technique.
Technical background
Nearly ten years, under the worldwide petrochemical energy increasingly exhausted situation, to the research of the recyclable organism substance energy into
For scientific and technological circle research hot spot, using the biomass resources such as vegetable and animals oils, gutter oil for raw material production biodiesel technology by
Majority state is grasped.The production of biodiesel scale, enlargement.The crude glycerine of biodiesel byproduct more than 10% is produced,
Comparison of ingredients is complicated.I.e. containing the light components such as low-boiling vegetable and animals oils, also containing salt, stearic acid and other high boiling heavy
The impurity such as component.Majority is purified using single column distillation technique both at home and abroad.Gained glycerine purity is below 96%.It can only use
Make the products such as industry glycerol, manufacture paint, and cannot be used for most of field such as daily-use chemical industry, medicine.To expand biodiesel
The use scope of by-product glycerol improves value of the product, studies a kind of production biodiesel byproduct crude glycerin high-purity purification technique
It is very important.
The content of the invention
The purpose of the present invention is being directed to production biodiesel byproduct crude glycerin at present, asking for high-purity glycerol can not be obtained
Topic provides a kind of production biodiesel byproduct crude glycerin high-purity purification technique.
Technical solution：To achieve the above object, this invention takes following technical solutions：
A kind of extraction process for producing biodiesel byproduct high purity extractive glycerine, comprises the following steps：
1st, flow is evaporated in vacuo using double tower：Pre-distillation is boiled off except light group of the low boiling points such as the moisture in crude glycerine and vegetable and animals oils
（1）Point, destilling tower extraction high purity extractive glycerine（2）, the high-boiling components desalination removal of impurities of distillation tower reactor precipitation（3）.
Biodiesel byproduct crude glycerin pump squeezes into pre-distillation column tower body top, is uniformly distributed by swirl injector,
Heat exchange, a small amount of glycerine of uprising gas entrainment are carried out with water in uphill process and animals and plants light component gasifying gas counter current contacting
Gas, which is condensed, returns to tower reactor, while crude glycerine is preheated.The low boiling point water and animals and plants gas not being condensed enter from tower top
Condenser（Ⅰ）Ground groove is discharged into after condensation（A）.Not vaporized glycerine and a small amount of stearic acid in pre-distillation tower reactor, salinity and
Other impurities pump squeezes into destilling tower tower body top, is uniformly distributed by swirl injector.It is sweet with rising through packing layer
Oil vapour counter current contacting, a small amount of stearic acid, salinity and the other impurities carried secretly in gas are brought back in distillation tower reactor, glycerin gas
Then condenser is discharged into from tower top（Ⅱ）Ground groove is discharged into after being condensed（B）.Not vaporized stearic acid, salt in destilling tower tower reactor
Divide and the suspension of other impurities composition is discharged into desalination, decleaning tank.In desalination, decleaning tank blowpipe and transverse direction are turned over equipped with vertical steam
Steam turns over blowpipe.High-pressure and high-temperature steam blows suspension from steam inlet into the horizontal, vertical uniformly distributed circular hole of blowpipe that turns over, and is allowed to turn over
It rises, wash away, diluting, melting, its liquid, through filter assemblies, is discharged into storage tank, to recycle firmly under suction function from tank bottom outlet
The organic matters such as resin acid, salt grain are then blocked on filter plate upper surface, are periodically taken out from fast open type manhole, as industrial salt.
Steam (vapor) outlet connects flash tank, and flash tank liquid-phase outlet connects hot-water line back boiler, and gaseous phase outlet connects pre-distillation column tower reactor
Heater inlet pipe, to achieve the purpose that UTILIZATION OF VESIDUAL HEAT IN is energy saving.
2nd, capital equipment：
Destilling tower tectonic sieving is to be configured to include：Tower reactor, tower reactor is interior to place spiral coil heater, the direct-connected tower body of tower reactor.
Tower body top sets material inlet, connects swirl injector.Injector Intalox metal tower packing layer arranged below, tower top set glycerin gas
Outlet, connects condenser, and condenser is shell and tube water cooler.Condensate outlet sets threeway, and one connects vacuum system, secondly ground connection
Face groove.
Coil heater wound with high temperature resistant stainless steel pipe it is spiral, to increase heat exchange area, shared by reduction
Space, convenient for gasification separation.
Swirl injector is one of core technology of the present invention, is internally provided with helical duct and spout assembly, can will be sticked
It is uniform to spend larger material sprinkling, is come into full contact with beneficial to gas-liquid two-phase, improves heat exchange and separative efficiency.
Two-step distillation process of the present invention uses TQK automatic control systems：Using TQK controllers.
Including：TQ computing units, control module, human-machine interface module, fieldbus module.Temperature, flow node control
Device, executing agency, executing agency is containing temperature electrode, flow electrode, solenoid valve etc..TQ computing units are connected with control module, are used
In the temperature, flow control parameter generation temperature, flow control signal that are stored according to control module；Human-machine interface module and control
Module connects, for live design temperature, flow parameter.Fieldbus module is connected with control module, for all temperature,
Flow Node Controller sends instruction and receives operating status；All temperature, flow Node Controller are connected with executing agency, are used
In control and temperature, flow are adjusted in the process parameters range of setting.
Description of the drawings
Attached drawing 1 shows the structure diagram of destilling tower；Attached drawing 2 shows the structure diagram of desalination, decleaning tank；Attached drawing
3 show a kind of production biodiesel byproduct crude glycerin high-purity purification process flow diagram.
Specific embodiment
Below in conjunction with the accompanying drawings 1, attached drawing 2, attached drawing 3 are described further.
Embodiment
As shown in Figure 1：The construction of destilling tower mainly includes：Low head 1, upper cover 2, coil heater 3, autoclave body
4th, tower body 5, filler 6, tower body end socket 7, smart glycerin vapor outlet 8, glycerine and heavy constituent inlet tube 9, glycerine and restructuring shunting
Measure Node Controller 10, steam outlet pipe 11, bottom temperature thermal detector 12, steam inlet pipe 13, steam flow Node Controller
14th, impurity and heavy constituent discharge pipe 15, manhole 16.
Select DN1600PN1.6MPa stainless steels upper cover 1, low head 2, Volume soldering stainless steel materials Φ 1600 × 10
×16000（h）Tower body 3, be welded as a whole with 2 low head 1 of upper cover.Φ 800mm circular holes are opened at 2 center of upper cover, in circle
Φ 800 × 8 × 16000 is welded at hole（h）Tower body 5.Apart from 1.5 meters of place's filling Intalox metal tower packings of tower reactor in the tower body 5（6）It is high by 8
Rice, on tower body top, welding tower body end socket 7,100 circular holes of Φ are opened at 7 end socket center of tower body, weld smart 8 Φ of glycerin vapor outlet
108 × 2 × 200, open 100 circular holes of Φ welding Φ 108 × 3 × 300 for 1.5 meters far from top in tower body one side（It is long）Glycerine and heavy constituent
Feed pipe 9, installation steam flow Node Controller 10 in the middle part of pipe, steam is welded in tower reactor away from perforate at upper cover 2400mm herein
Inlet tube 12 is Φ 57 × 3 × 200（It is long）, and be connected with kettle inside spin coil heater 3, steam stream is installed in the middle part of pipe herein
Measure Node Controller 14.The perforate installation temperature thermal detector 13 in the middle part of tower reactor, away from low head 400mm at perforate weld Φ 57 ×
3×300（It is long）Steam outlet pipe 11, and be connected with tower reactor inside spin coil heater, weld Φ in 1 center drilling of low head
108 × 4 × 200 heavy constituents and impurity blow-off pipe 15 install manhole 16 for overhauling respectively in tower reactor and tower body.
The making of desalination decleaning tank：As shown in Figure 2
The construction of desalination decleaning tank includes：Stent 1, steam inlet pipe 2, cylinder 3, blow-down pipe 4, feed pipe 5, upper cover 6, Jia Shui
Pipe 7, upper and lower visor 8, steam laterally turn over blowpipe 9, steam and vertically turn over blowpipe 10, fast open type manhole 11, filter assemblies 12, low head
13rd, feed opening 14.
DN1200PN1.6MPa upper covers 6, low head 13 are chosen, with Φ 1200 × 3 × 2500（h）Cylinder 3 is welded.
In cylinder one side away from 600 circular holes of Φ are opened at low head 200mm, fast open type manhole 11 is installed, in cylinder opposite side away from low head
Φ 50mm circular holes welding steam inlet pipe 2 is opened at 200mm and laterally turns over 9 steam of blowpipe with steam in cylinder and vertically turns over blowpipe 10 and is connected
It connects.It laterally turns over blowpipe and is erected in body centre and be evenly distributed with 5 circular holes of Φ.Steam vertically turns over blowpipe and lies against body centre, circumference uniform distribution
5 circular holes of Φ.In cylinder opposite side Φ 57 × 3 × 150 is welded away from perforate at upper cover 200mm（It is long）Filler pipe 7, in upper cover 6
Center drilling welds Φ 108 × 3 × 200（It is long）Feed pipe 5 welds Φ 108 × 3 × 200 in low head center drilling（It is long）Under
Expects pipe 14, in upper cover deviation perforate welding Φ 37 × 2 × 150（It is long）Drain 4, in cylinder one side away from being opened at low head 1.5m
Upper and lower visor 8 is installed, three stents 1 are finally installed around low head in hole.
A kind of production biodiesel byproduct crude glycerin high-purity purification technique is as shown in Figure 3：A kind of production biodiesel pair
Crude glycerine high-purity extraction process is produced, is comprised the following steps：Pre-distillation removes moisture and light component substance 1；Rectifying extraction is high-purity
The smart glycerine 2 of degree；Higher boiling heavy constituent desalination removal of impurities 3；The automation 4 of operating process.
Step pre-distillation removes moisture and low boiling point light component substance 1, detailed process：It is slightly sweet to produce biodiesel byproduct
Oil squeezes into the in vivo swirl injector of tower with pump from crude glycerine import.It crude glycerine is evenly distributed with sprinkling nebulizes down and drop down onto tower reactor
It is interior, the steam from destilling tower tower reactor heater enter from steam inlet crude glycerine in spiral disc type heater heating kettle to
150 DEG C, water and low boiling component gasification in crude glycerine rise the crude glycerine counter current contacting with falling along tower body inside.Low boiling
The water and light component steam of point are not condensed, and continue uplink and are discharged into water condenser from light-component gas outlet at the top of tower body, water
Steam and light component steam, which are condensed, is discharged into ground groove.The a small amount of glycerine in bottom is gasified on vapor in evaporation process
Row, when the low temperature crude glycerine with whereabouts contacts and is condensed and still falls in tower reactor, eliminate water and vegetable and animals oils in crude glycerine
Etc. light components.
Step rectifying extraction high purity extractive glycerine 2：Glycerine and higher boiling heavy constituent in pre-distillation column tower reactor are arranged from bottom of towe
Material mouth is discharged, and the glycerine on destilling tower top and heavy constituent inlet tube are squeezed by pump, is nebulized into swirl injector sprinkling,
Even to enter packing layer, the glycerin vapor counter current contacting slowly to fall with uplink is fallen into after preheating in tower reactor.
High-pressure steam enters coil heater from steam inlet pipe, glycerine and heavy constituent in heat tower reactor.
Along uplink inside tower body after glycerine gasification, by packing layer and the low temperature glycerine and heavy constituent counter current contacting that fall, hot friendship is carried out
It changes.Since glycerine relative boiling point is low, glycerin gas is not condensed, and entering water condenser from tower top glycerin vapor outlet is condensed
After be discharged into ground groove.Steam (vapor) outlet is directly discharged into flash tank, and liquid phase removes boiler, and gas phase water vapour is heated from pre-distillation column tower reactor
Device entrance enters pre-distillation column heater, UTILIZATION OF VESIDUAL HEAT IN.
Small part high boiling substance is gasified in evaporation process, and packing layer is risen to glycerin vapor, since it is opposite
Boiling point is higher, in packing layer and enters the low temperature glycerine of tower and heavy constituent counter current contacting.It is condensed and still falls back in tower reactor.It will not press from both sides
Band is allowed to glycerine purity more than 99.5 in glycerin vapor.
Step higher boiling heavy constituent desalination removal of impurities 3：Its process is to distill higher boiling heavy constituent in tower reactor from bottom discharge
Mouth discharge, is directly discharged into desalination decleaning tank.Be equipped in tank steam laterally, vertically turn over blowpipe, high-pressure and high-temperature steam from steam into
Pipe enters steam and vertically turns over blowpipe and laterally turn over blowpipe, is blown out from uniformly distributed circular hole, blows high-boiling components.Formation, which is seethed, washes away,
The dopes such as the stearic acid being adhered in salt grain are rinsed, are diluted, thawing is allowed to be kept completely separate with salt grain, the penetration by liquid of formation
Filter assemblies are discharged into storage tank to recycle the organic matters such as stearic acid from tank bottom outlet.Salt grain is then blocked on filter plate upper surface, periodically
It is taken out from fast open type manhole, as industrial salt.
The automation 4 of operating process：The operating process of the present invention is using new TQK controllers, the TQK controllers of development
Including TQ temperature, flow rate calculation unit, human-machine interface module, control module, fieldbus module, scene temperature, flow node
Controller and executing agency.
TQ computing units are connected with human-machine interface module, for live setup parameter；
TQ computing units are connected with control module, for generating temperature flow according to the humidity flow control parameter of control module storage
Measure control signal；Fieldbus module and control module and live flow, temperature nodes controller are connected, for all temperature
Degree, flow Node Controller send instruction and receive the instant operating status in scene；Field node controller is connected with executing agency,
For controlling to adjust, temperature, flow within the preset range.
150 DEG C, crude glycerine pre-distillation column flow 10m3/h of present invention setting pre-distillation column bottom temperature, input of column stream
Measure 9m3/h。
It is characteristic of the invention that the first step：Pre-distillation column removes the relatively low light component of boiling point, and it is miscellaneous to have prevented light component
Matter is mixed into glycerine in distillation process.It is miscellaneous that second step by rectifying column eliminates the relatively high high-boiling components of boiling point and salinity etc.
Matter avoids high-boiling components and is mixed into glycerin vapor, it is ensured that the high-purity of gained glycerine.3rd step by removing salt cellar, eliminates height
The salinity in the organic matters such as object stearic acid is boiled, the organic matters such as stearic acid and salinity is made all to be utilized.Most significant feature is this
Invention employs new TQ robot control system(RCS)s, realizes being precisely controlled for temperature and flow, it is ensured that the high-purity of product.
Claims (6)
1. a kind of production biodiesel byproduct crude glycerin high-purity extraction process, moisture removal and vegetable and animals oils etc. are removed including pre-distillation
Light component（1）；Distillation extraction high purity extractive glycerine（2）；Bottom high-boiling components desalination, removal of impurities（3）, it is characterised in that：Production biology
The crude glycerine of diesel oil by-product, which pumps, squeezes into pre-distillation column, and the coil pipe in tower reactor is passed through steam and heats crude glycerine to 155--160 DEG C,
The vaporizations such as remaining moisture and low-boiling vegetable and animals oils wherein in crude glycerine, condenser is discharged into from tower top（I）, after condensation
It is discharged into groove（A）, the high-boiling components such as glycerine and a small amount of stearic acid throw destilling tower tower body top by delivery pump in kettle, lead to from top to bottom
It crosses packing layer and enters tower reactor, the coil pipe in tower reactor is passed through steam, and glycerine in kettle and other materials are heated to 190--200 DEG C makes
Vaporization, gas contacted, low boiling point glycerin gas is discharged into cold from tower top by tower body packing layer with the liquid countercurrent into tower
Condenser（II）Groove is discharged into after being condensed（B）, high boiling stearic acid, salt and other impurity are condensed in tower body with into tower
Material returns to tower reactor and is deposited in bottom, periodically discharges, and the high-boiling components of discharge are through desalination, decleaning tank processing.
2. a kind of production biodiesel byproduct crude glycerin high-purity purification technique according to claim 1, it is characterised in that：Institute
State distillation extraction high-precision glycerine（2）, the construction of key equipment destilling tower includes：Tower reactor, tower reactor is interior to be added equipped with coil
Equipped with swirl injector, Intalox metal tower packing, temperature, automatic flow control system etc. in hot device, tower body, tower body.
3. a kind of production biodiesel byproduct crude glycerin high-purity purification technique according to claim 1, it is characterised in that：Institute
State bottom high-boiling components desalination, removal of impurities（3）, key equipment desalination, decleaning tank, constructing includes：Tank body, upper low head, steam into
Mouth pipe, steam vertically turn over blowpipe, steam and laterally turn over blowpipe, filter pack, and upper and lower visor unloads salt hole, liquid impurity feed opening
Deng.
4. a kind of production biodiesel byproduct crude glycerin high-purity purification technique according to claim 2, it is characterised in that：Institute
It states in the tower reactor of destilling tower equipped with spiral coil heater, helical coiled tube is wound in more high temperature resistant stainless steel pipes, exchange heat
Area is big, takes up space small, beneficial to the heating of thick liquid.
5. a kind of production biodiesel byproduct crude glycerin high-purity purification technique according to claim 2, it is characterised in that：Institute
Equipped with swirl injector in the construction tower body for the destilling tower stated, it is special that injector interior is equipped with helical duct, spout assembly etc.
Structure, the crude glycerine for enabling viscosity larger uniformly spray, and contact, are filled with the water and light component steam counter-flow of uplink in tower body
The heat exchange divided.
6. a kind of production biodiesel byproduct crude glycerin high-purity purification technique according to claim 3, it is characterised in that：Institute
The construction of destilling tower is stated, including temperature, automatic flow control system, employs TQK controllers, including TQ computing units, control
Module, human-machine interface module, fieldbus module, TQ computing units are connected with control module, for being stored according to control module
Temperature, flow control parameter generate temperature, flow control signal；Human-machine interface module is connected with control module, for scene
Design temperature, flow parameter, fieldbus module are connected with control module, for being sent out to all temperature, flow Node Controller
It send instruction and receives operating status；All Node Controllers are connected with executing agency, and for controlling and adjusting temperature, flow is being set
In fixed process parameters range.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810016944.6A CN108069828A (en) | 2018-01-09 | 2018-01-09 | A kind of production biodiesel byproduct crude glycerin high-purity purification technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810016944.6A CN108069828A (en) | 2018-01-09 | 2018-01-09 | A kind of production biodiesel byproduct crude glycerin high-purity purification technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108069828A true CN108069828A (en) | 2018-05-25 |
Family
ID=62156536
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810016944.6A Pending CN108069828A (en) | 2018-01-09 | 2018-01-09 | A kind of production biodiesel byproduct crude glycerin high-purity purification technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108069828A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109293476A (en) * | 2018-11-29 | 2019-02-01 | 浙江工业大学 | Glycerol separating technology and device in a kind of glycerine esterification production waste water |
| CN112121452A (en) * | 2020-09-27 | 2020-12-25 | 江苏科技大学 | Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation |
| CN112457168A (en) * | 2021-01-07 | 2021-03-09 | 浙江工业大学 | Resource treatment method for biodiesel byproduct salt-containing crude glycerol |
| CN114681943A (en) * | 2022-03-16 | 2022-07-01 | 中国石油化工股份有限公司 | Method for heating cumene recovery tower |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201106041Y (en) * | 2007-07-26 | 2008-08-27 | 占小玲 | Device for one-step synthesis of biodiesel and alcohol radical fuel under atmospheric temperature and normal pressure |
| CN101358140A (en) * | 2007-08-02 | 2009-02-04 | 姜皓 | Synthetic process of bio diesel oil and equipment |
| CN101735845A (en) * | 2008-11-10 | 2010-06-16 | 北京化工大学 | Method for separating and purifying biodiesel |
| CN102260141A (en) * | 2010-05-25 | 2011-11-30 | 中国林业科学研究院林产化学工业研究所 | Production method and device of refined glycerin in non-distillation techniques |
| CN102432429A (en) * | 2011-08-26 | 2012-05-02 | 佛山汉维机电科技有限公司 | Method for recovering glycerin and polyglycerol from raffinate obtained after preparing refined glycerin through distillation |
| CN103468413A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
| CN104818125A (en) * | 2015-05-04 | 2015-08-05 | 浙江大学 | Method for using waste oil and grease as raw material to prepare fatty acid methyl ester |
| CN204637028U (en) * | 2015-04-24 | 2015-09-16 | 四川科伦药业股份有限公司 | Reduce fat milk peroxide value and anisidine value processing system |
| CN106083526A (en) * | 2016-06-01 | 2016-11-09 | 金河生物科技股份有限公司 | Ethanol reclaims the system and method for Automated condtrol |
| CN106187689A (en) * | 2016-08-10 | 2016-12-07 | 天津大学 | A kind of method of continuous purification crude glycerine |
-
2018
- 2018-01-09 CN CN201810016944.6A patent/CN108069828A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201106041Y (en) * | 2007-07-26 | 2008-08-27 | 占小玲 | Device for one-step synthesis of biodiesel and alcohol radical fuel under atmospheric temperature and normal pressure |
| CN101358140A (en) * | 2007-08-02 | 2009-02-04 | 姜皓 | Synthetic process of bio diesel oil and equipment |
| CN101735845A (en) * | 2008-11-10 | 2010-06-16 | 北京化工大学 | Method for separating and purifying biodiesel |
| CN102260141A (en) * | 2010-05-25 | 2011-11-30 | 中国林业科学研究院林产化学工业研究所 | Production method and device of refined glycerin in non-distillation techniques |
| CN102432429A (en) * | 2011-08-26 | 2012-05-02 | 佛山汉维机电科技有限公司 | Method for recovering glycerin and polyglycerol from raffinate obtained after preparing refined glycerin through distillation |
| CN103468413A (en) * | 2013-09-25 | 2013-12-25 | 陕西合盛生物柴油技术开发有限公司 | Production method of biodiesel |
| CN204637028U (en) * | 2015-04-24 | 2015-09-16 | 四川科伦药业股份有限公司 | Reduce fat milk peroxide value and anisidine value processing system |
| CN104818125A (en) * | 2015-05-04 | 2015-08-05 | 浙江大学 | Method for using waste oil and grease as raw material to prepare fatty acid methyl ester |
| CN106083526A (en) * | 2016-06-01 | 2016-11-09 | 金河生物科技股份有限公司 | Ethanol reclaims the system and method for Automated condtrol |
| CN106187689A (en) * | 2016-08-10 | 2016-12-07 | 天津大学 | A kind of method of continuous purification crude glycerine |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109293476A (en) * | 2018-11-29 | 2019-02-01 | 浙江工业大学 | Glycerol separating technology and device in a kind of glycerine esterification production waste water |
| CN112121452A (en) * | 2020-09-27 | 2020-12-25 | 江苏科技大学 | Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation |
| CN112457168A (en) * | 2021-01-07 | 2021-03-09 | 浙江工业大学 | Resource treatment method for biodiesel byproduct salt-containing crude glycerol |
| CN114681943A (en) * | 2022-03-16 | 2022-07-01 | 中国石油化工股份有限公司 | Method for heating cumene recovery tower |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108069828A (en) | A kind of production biodiesel byproduct crude glycerin high-purity purification technique | |
| CN102295564A (en) | Continuous production process for DOP (Dioctyl Phthalate) and used equipment | |
| CN102512835A (en) | Multi-effect plate type rising film countercurrent evaporation concentration device and method thereof | |
| CN108607232B (en) | Distillation device | |
| CN1679993A (en) | Continuous high-efficient vacuum concentration of Chinese medicine soup and apparatus thereof | |
| CN201603410U (en) | Energy-saving continuous alcohol-rectification recovery tower | |
| CN102512833A (en) | Horizontal-pipe falling-film evaporation method coupling distillation and device thereof | |
| CN208611833U (en) | Multi-stage distillation equipment | |
| KR100243518B1 (en) | A distillation apparatus for high purity distilled water manufacture | |
| CN202315342U (en) | Horizontal pipe falling film evaporation tower | |
| CN101954198A (en) | High-pressure dehydrating tower in process of continuously producing trimellitate | |
| CN100503787C (en) | Vertical film flash distillation rectifying still for producing bio diesel fuel | |
| CN214167408U (en) | Treatment device for treating low-concentration wastewater by using waste heat of condensed water | |
| CN205832659U (en) | Ethylene glycol distills multistage energy recovery system | |
| CN102453008B (en) | Novel process for preparing furfural by two towers and dedicated comprehensive tower | |
| CN204699421U (en) | A kind of refining plant of trioctyl trimellitate (TOTM) | |
| CN104803828B (en) | Device and method for improving 1,4-butanediol yield | |
| CN200967802Y (en) | Bitumen purification tower | |
| CN107141199A (en) | Methanol mother liquor is without refluxed cryogenic rectificating method and equipment | |
| CN207451656U (en) | A kind of continuous removal of ammonia and nitrogen light component organic matter and salt system | |
| CN101927096B (en) | Wire ball micro-filler decompression evaporator and use method thereof | |
| CN205933695U (en) | Methyl alcohol mother liquor does not have backward flow low temperature rectification plant | |
| CN111349011A (en) | Continuous esterification fractionation equipment and method for synthesizing butyl oleate and butyl palmitate | |
| CN102309866A (en) | Treating column of cyclic 1, 3-propanediol in continuous production process of poly (trimethylene terephthalate) | |
| CN219342073U (en) | Diesel oil regasification device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20180525 |
|
| WD01 | Invention patent application deemed withdrawn after publication |