CN108671575A - superheated steam stripping system - Google Patents
superheated steam stripping system Download PDFInfo
- Publication number
- CN108671575A CN108671575A CN201810687833.8A CN201810687833A CN108671575A CN 108671575 A CN108671575 A CN 108671575A CN 201810687833 A CN201810687833 A CN 201810687833A CN 108671575 A CN108671575 A CN 108671575A
- Authority
- CN
- China
- Prior art keywords
- superheated steam
- superheater
- air inlet
- distillation still
- inlet pipe
- 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
- 238000004821 distillation Methods 0.000 claims abstract description 31
- 239000007791 liquid phase Substances 0.000 claims abstract description 27
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 17
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- 239000007792 gaseous phase Substances 0.000 claims abstract description 11
- 239000002994 raw material Substances 0.000 claims abstract description 5
- 239000007789 gas Substances 0.000 claims description 27
- 239000012071 phase Substances 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 17
- 238000003756 stirring Methods 0.000 claims 1
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 229920000642 polymer Polymers 0.000 abstract description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 239000002199 base oil Substances 0.000 description 4
- 230000008676 import Effects 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- 239000012530 fluid Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000004615 ingredient Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 210000003205 muscle Anatomy 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Classifications
-
- 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
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a kind of superheated steam stripping systems, including stripping distillation still and superheater；The stripping distillation still top side is provided with feedstock oil feed inlet and feed distributor, the top other side is provided with superheated steam air inlet pipe, the superheated steam distributor that the air inlet pipe passes through distillation autoclave body to be arranged with lower part in autoclave body is connect, the superheater air inlet connects saturated vapor device for making, and the superheater is connect with stripping distillation still air inlet pipe.It is equipped with control valve and flowmeter on the raw material oil inlet, liquid-phase outlet, gaseous phase outlet and steam inlet duct.It is provided with agitating device in the distillation still.The heating selection of the heating tube is controllable.It is the system reasonable design, easy to use, effectively the light component in polymer can be separated, improve the flash-point of product, viscosity and other comprehensive performances.Production cost is reduced simultaneously, has largely saved the consumption of the energy.
Description
Technical field
Superheated steam stripping system of the present invention, belongs to base oil processing techniques field.
Background technology
The purification of synthetic base oil uses always nitrogen air lift, and it is huge that nitrogen air lift not only consumes nitrogen amount, but also air lift
It is ineffective, it causes product quality very different, largely affects the quality of product.Then saturated vapor vapour is used again
It carries, from product quality, although improving much, also achieves many achievements, the temperature of saturated vapor is relatively low, in gas
The temperature that synthetic base oil is reduced during carrying is unfavorable for the fast eliminating of light component.
Invention content
To solve the shortcomings of the prior art, the invention discloses a kind of superheated steam stripping system, system designs
Rationally, easy to use, effectively the light component in polymer can be separated, improve the flash-point of product, viscosity and its
His comprehensive performance.Production cost is reduced simultaneously, has largely saved the consumption of the energy.
Superheated steam stripping system of the present invention, including stripping distillation still and superheater；The stripping distillation still top side
It is provided with feedstock oil feed inlet and feed distributor, the top other side is provided with superheated steam air inlet pipe, and the air inlet pipe passes through
Distillation autoclave body is connect with the superheated steam distributor that lower part in autoclave body is arranged, and gaseous phase outlet, kettle are provided at the top of the distillation still
Bottom is provided with liquid-phase outlet；The gaseous phase outlet connects gas phase storage tank through gas phase heat exchanger；The liquid-phase outlet is changed through liquid phase
Hot device connects liquid phase storage tank；
The superheater includes heating tube, air inlet and gas outlet, and the air inlet connects saturated vapor device for making, it is described go out
It is additionally provided with a steam-water separator outside gas port, a temperature sensor is set in the superheater cavity；
The superheater is connect with stripping distillation still air inlet pipe.
It is equipped with control valve and flowmeter on the raw material oil inlet, liquid-phase outlet, gaseous phase outlet and steam inlet duct.
The gas phase heat exchanger and liquid phase heat exchanger are set to the hot water inlet pipe road of saturated vapor device for making.
It is provided with agitating device in the distillation still.
The heating selection of the heating tube is controllable.
A leakage fluid dram is arranged in the superheater bottom.
The present invention has the advantages that compared with prior art：
It is the system reasonable design, easy to use, effectively the light component in polymer can be separated, improve the sudden strain of a muscle of product
Point, viscosity and other comprehensive performances.Production cost is reduced simultaneously, has largely saved the consumption of the energy.
Description of the drawings
Fig. 1 is the structural diagram of the present invention；
In figure：1 is distillation still, and 2 be superheater, and 3 be agitating device, and 4 be hot water inlet pipe road, and 10 be feedstock oil feed inlet, 11
It is air inlet pipe for feed distributor, 12,13 be distributor, and 14 be gaseous phase outlet, and 15 be liquid-phase outlet, and 16 be gas phase heat exchanger,
17 be gas phase storage tank, and 18 be liquid phase heat exchanger, and 19 be liquid phase storage tank, and 20 be saturated vapor device for making, and 21 be heating tube, and 22 are
Air inlet, 23 be gas outlet, and 24 be steam-water separator, and 25 be temperature sensor, and 26 be leakage fluid dram, and 30 be control valve, and 31 are
Flowmeter.
Specific implementation mode
With reference to specific embodiments and the drawings, the present invention is described in further detail, but the protection model of the present invention
It encloses and is not limited to these examples, every protection that the present invention is included in without departing substantially from the change of present inventive concept or equivalent substitute
Within the scope of.
As shown in Figure 1,
Superheated steam stripping system, including stripping distillation still 1 and superheater 2；The 1 top side of stripping distillation still is provided with original
The oily feed inlet 10 of material and feed distributor 11, the top other side are provided with superheated steam air inlet pipe 12, and the air inlet pipe 12 passes through
Distillation autoclave body is connect with the superheated steam distributor 13 that lower part in autoclave body is arranged, and 1 top of the distillation still is provided with gaseous phase outlet
14, bottom portion is provided with liquid-phase outlet 15；The gaseous phase outlet 14 connects gas phase storage tank 17 through gas phase heat exchanger 16；The liquid phase
Outlet 15 connects liquid phase storage tank 19 through liquid phase heat exchanger 18；
The superheater 2 includes heating tube 21, air inlet 22 and gas outlet 23, and the air inlet 22 connects saturated vapor and produces dress
20 are set, a steam-water separator 24 is additionally provided with outside the gas outlet 23, a temperature sensor 25 is set in the superheater cavity；
The operation of heating tube can be controlled according to temperature conditions.
The superheater 2 is connect with stripping distillation still air inlet pipe 12.
It is equipped with control valve on the raw material oil inlet 10, liquid-phase outlet 15, gaseous phase outlet 14 and steam inlet duct 12
30 and flowmeter 31.It can play the role of adjusting flow.
The gas phase heat exchanger 16 and liquid phase heat exchanger 18 are set to the hot water inlet pipe road 4 of saturated vapor device for making 20
On.
Agitating device 3 is provided in the distillation still 1.
A leakage fluid dram 26 is arranged in the superheater bottom.
Superheated steam gas stripping process, includes the following steps：
Saturated vapor is inputted into superheater import, superheater outlet is connected to bottom in distillation still；
Condensed water in superheater is exhausted, superheater heating tube is started, heating saturated vapor makes its temperature reach 220-260
DEG C, become superheated steam；
Superheated steam is after steam-water separator detaches, then opens the superheated steam import tube valve of distillation still, and distillation still starts vapour
It carries；
The gas phase composition generated after stripping is exported by distillation still top gas phase and is discharged, and entering gas phase after the heat exchange of gas phase heat exchanger stores up
Tank is collected；The liquid phase ingredient generated after stripping is collected after the heat exchange of liquid phase heat exchanger by liquid phase storage tank；
The gas phase heat exchanger and liquid phase heat exchanger, by heat heat exchange to hot water inlet pipe, the hot water in hot water inlet pipe is logical
Enter saturated vapor device for making and produces saturated vapor.
In actual use, saturated vapor is inputted into superheater import,.In stripping, first the condensed water in superheater is arranged
Fall, starts heating tube, saturated vapor is heated to superheated steam, temperature reaches 220-260 DEG C, then opens the mistake of distillation still again
Hot steam import tube valve, distillation still start to strip.The gas phase composition and liquid phase ingredient generated after stripping is after heat exchanger exchanges heat
It collects, is further processed, heat exchanger exchanges heat heat into hot water inlet pipe, and hot water therein enters saturated vapor device for making
Produce saturated vapor.
A steam-water separator is additionally provided with outside the gas outlet of superheater so that the superheated steam moisture-free of generation ensures
Steam stripped effect.
The setting of feed distributor and superheated steam distributor in distillation still, makes raw material and superheated steam come into full contact with, carries
The high efficiency of separation base oil light component, saves the production time.
The present invention is not limited by embodiment illustrated herein, and is to fit to and principles disclosed herein and novelty
The consistent widest range of feature.
Claims (6)
1. superheated steam stripping system, which is characterized in that including stripping distillation still（1）And superheater（2）；The stripping distillation still
（1）Top side is provided with feedstock oil feed inlet（10）And feed distributor（11）, the top other side be provided with superheated steam into
Tracheae（12）, the air inlet pipe（12）Across the superheated steam distributor of distillation autoclave body and lower part setting in autoclave body（13）Connection,
The distillation still（1）Top is provided with gaseous phase outlet（14）, bottom portion is provided with liquid-phase outlet（15）；The gaseous phase outlet（14）
Through gas phase heat exchanger（16）Connect gas phase storage tank（17）；The liquid-phase outlet（15）Through liquid phase heat exchanger（18）Connect liquid phase storage tank
（19）；
The superheater（2）Including heating tube（21）, air inlet（22）The gas outlet and（23）, the air inlet（22）Connection saturation
Steam device for making（20）, the gas outlet（23）It is additionally provided with a steam-water separator outside（24）, set in the superheater cavity
Set a temperature sensor（25）；
The superheater（2）With stripping distillation still air inlet pipe（12）Connection.
2. superheated steam stripping system according to claim 1, it is characterised in that：The raw material oil inlet（10）, liquid phase
Outlet（15）, gaseous phase outlet（14）With superheated steam air inlet pipe（12）On be equipped with control valve（30）And flowmeter（31）.
3. superheated steam stripping system according to claim 1, it is characterised in that：The gas phase heat exchanger（16）And liquid phase
Heat exchanger（18）It is set to saturated vapor device for making（20）Hot water inlet pipe road（4）On.
4. superheated steam stripping system according to claim 1, it is characterised in that：The distillation still（1）It is inside provided with and stirs
Mix device（3）.
5. superheated steam stripping system according to claim 1, it is characterised in that：The heating tube（21）Heating can
Control.
6. superheated steam stripping system according to claim 1, it is characterised in that：A drain is arranged in the superheater bottom
Mouthful（26）.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810687833.8A CN108671575A (en) | 2018-06-28 | 2018-06-28 | superheated steam stripping system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810687833.8A CN108671575A (en) | 2018-06-28 | 2018-06-28 | superheated steam stripping system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108671575A true CN108671575A (en) | 2018-10-19 |
Family
ID=63812602
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810687833.8A Pending CN108671575A (en) | 2018-06-28 | 2018-06-28 | superheated steam stripping system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108671575A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109897124A (en) * | 2019-04-28 | 2019-06-18 | 扬州天诗新材料科技有限公司 | A kind of preparation facilities and preparation method of continous way purification polyethylene wax |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201735198U (en) * | 2009-12-16 | 2011-02-09 | 曲靖众一精细化工股份有限公司 | Small efficient steam-stripping separating device |
| CN208511901U (en) * | 2018-06-28 | 2019-02-19 | 山西潞安纳克碳一化工有限公司 | A kind of superheated steam stripping system |
-
2018
- 2018-06-28 CN CN201810687833.8A patent/CN108671575A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201735198U (en) * | 2009-12-16 | 2011-02-09 | 曲靖众一精细化工股份有限公司 | Small efficient steam-stripping separating device |
| CN208511901U (en) * | 2018-06-28 | 2019-02-19 | 山西潞安纳克碳一化工有限公司 | A kind of superheated steam stripping system |
Non-Patent Citations (1)
| Title |
|---|
| 石油化工科学研究院综合研究所情报室 编: "《流化催化裂化》", 中国工业出版社出版, pages: 136 - 137 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109897124A (en) * | 2019-04-28 | 2019-06-18 | 扬州天诗新材料科技有限公司 | A kind of preparation facilities and preparation method of continous way purification polyethylene wax |
| CN109897124B (en) * | 2019-04-28 | 2022-04-22 | 扬州天诗新材料科技有限公司 | Continuous preparation device and preparation method of refined polyethylene wax |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107008026B (en) | Nickel sulfate evaporative crystallization technique | |
| CN207785960U (en) | Energy-saving concentration unit | |
| CN104922921B (en) | A kind of self-loopa MVR thermo-compression evaporation systems | |
| CN204522347U (en) | A kind of solvent distillation recovery device | |
| CN206861916U (en) | A kind of HEAT PUMP BASED ON EJECTING PRINCIPLE residual heat resources retracting device of vegetable protein flash-off steam | |
| CN108671575A (en) | superheated steam stripping system | |
| CN105732316B (en) | A kind of purification of glycerin system | |
| CN207418323U (en) | A kind of split type condensing unit | |
| CN206278948U (en) | A kind of micro- aeration solar energy pressure reducing film distillation haline water desalt processing system | |
| CN208511901U (en) | A kind of superheated steam stripping system | |
| CN202538386U (en) | Alcohol recovery tower | |
| CN206027148U (en) | High -efficient plant is drawed and uses membrane concentrator | |
| CN203494188U (en) | Double-effect concentrator | |
| CN206396157U (en) | A kind of perfume purifies distilling apparatus | |
| CN205925063U (en) | Traditional chinese medicine draws canning and puts | |
| CN205690902U (en) | A kind of boiler circuit | |
| CN205627127U (en) | MVR triple -effect evaporator | |
| CN205235415U (en) | Thermal cycle mechanical compression evaporation plant | |
| CN207775182U (en) | A kind of orange oil distillation processing concentrator | |
| CN208823967U (en) | A kind of glycerol distillation device | |
| CN209383739U (en) | A kind of acidification oil hydrolysis device | |
| CN2726696Y (en) | Composite type Chinese medicinal liquid concentrating and alcohol reclaiming device | |
| CN204265469U (en) | A kind of negative pressure ammonia still | |
| CN208177003U (en) | Heat-preserving and energy-saving distillation device | |
| CN208809486U (en) | A kind of multi-cycle enrichment facility applied to soup-stock production |
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 | ||
| CB02 | Change of applicant information | ||
| CB02 | Change of applicant information |
Address after: 046100 Yuwu Town, Tunliu District, Changzhi City, Shanxi Province (east of Yuwu town government) Applicant after: Shanxi Lu'an carbon one chemical Co., Ltd Address before: 046100 Shanxi city of Changzhi province Tunliu County Yu Wu Zhen Applicant before: SHANXI LU'AN NAKE TANYI CHEMICAL CO., LTD. |