CN102225239A - Multilevel heat-exchange distilling device for dreggy organic materials - Google Patents
Multilevel heat-exchange distilling device for dreggy organic materials Download PDFInfo
- Publication number
- CN102225239A CN102225239A CN2011101313404A CN201110131340A CN102225239A CN 102225239 A CN102225239 A CN 102225239A CN 2011101313404 A CN2011101313404 A CN 2011101313404A CN 201110131340 A CN201110131340 A CN 201110131340A CN 102225239 A CN102225239 A CN 102225239A
- Authority
- CN
- China
- Prior art keywords
- raw material
- jar
- heat
- heat exchanger
- preheating
- 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
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to the field of distilling and purification for dreggy organic materials, particularly to a multilevel heat-exchange distilling device for dreggy organic materials. The multilevel heat-exchange distilling device comprises a raw material storage jar, a raw material preheating jar, a raw material evaporating jar, a collecting device, a heating device, and a desulfuration dust-removing device, wherein the collecting device is connected with the raw material storage jar; the heating device is connected with the raw material evaporating jar; the desulfuration dust-removing device is communicated with the heating device; a discharge outlet of the raw material evaporating jar is connected with the collecting device through an evaporation discharging pipeline; and raw materials in the raw material storage jar are communicated with the raw material preheating jar through the discharge outlet of the raw material storage jar by virtue of a preheated material conveying pipeline and a second level condensation heat exchanger. Compared with the prior art, by collecting heat in the second level condensation heat exchanger, the raw materials are preheated and heated evaporating media are cooled, thereby saving preheating energy resource for the raw materials, saving a cooling resource for the heated evaporating media, and increasing the processing efficiency of the device.
Description
Technical field
The present invention relates to the distillation purification field of dirty organic materials, particularly a kind of dirty organic materials multi-stage heat exchanger distilling apparatus.
Background technology
The definition of dirty organic materials is according to being: contain other impurity, the organic matter of coking easily in the still-process that is heated.
Dirty organic materials comprising: contain the oil of other impurity or contain the impurity of oil, as used oil, solvent slop etc.
Be example with above-mentioned used oil below, distill purification processes.
The following two kinds of methods of the general employing of tradition used oil distillation:
One, tube furnace heating: used oil is packed in the evaporimeter with tubular boiler coil pipe internal communication, carry out body circulation heating, after the temperature that obtains to make oil content evaporation in it, make oil content steam raising in it.
Two, kiln formula heating: evaporimeter is placed in the kiln body of bottom fire coal, used oil is packed in the evaporimeter, obtain evaporation heat, after the temperature that obtains to make oil content evaporation in it, make oil content steam raising in it by the coal-fired heat release in bottom.
The defective that said method exists is:
One, tube furnace heating: this method is heated directly, and energy consumption is lower, but because of used oil contains a large amount of impurity, when used oil constantly is heated after, be very easy to it in the impurity coking in boiler tube, make its boiler tube circulation area constantly decline until obstruction.
Two, kiln formula heating: this method is heated directly, can remove the coking material that remains in evaporimeter inside easily, but relatively simple for structure because of being heated of kiln body heating, the evaporimeter heat exchange area is less, and the energy consumption of this method is higher thus, working (machining) efficiency is lower.
Summary of the invention
The objective of the invention is to overcome the deficiency of background technology, is raw material and a kind of waste heat of can gathering is provided
Carry out the dirty organic materials multi-stage heat exchanger distilling apparatus of preheating.
The present invention solves its technical problem and adopts following technical scheme:
A kind of dirty organic matter multi-stage heat exchanger distilling apparatus, comprise raw material storage jar, the raw material preheating jar, the raw materials evaporate jar, with the raw material tank connected gathering-device of storing in a warehouse, with the tank connected heating combined equipment of raw materials evaporate, the desulfation dust-extraction device that is communicated with heating combined equipment, the floss hole of described raw materials evaporate jar is connected with gathering-device by the discharge vaporization pipeline; A described raw material storage jar interior raw material is communicated with the raw material preheating jar through preheating material feed-line and B-grade condensation heat exchanger by its discharge gate.
The present invention of employing technique scheme compared with prior art, raw material is by gathering the heat in the B-grade condensation heat exchanger, not only can make raw material realize preheating, can also make the evaporative medium that is heated realize cooling, not only saved the pre-heat energy of raw material thus, also save the cooling resource of the evaporative medium that is heated, also improved the working (machining) efficiency of device.
As a preferred embodiment of the present invention, described its discharge gate of raw material preheating jar passes through the hot charge feed-line again and is communicated with the evaporator feeding mouth through the one-level condensing heat exchanger.
As a preferred embodiment of the present invention, described heating combined equipment is a thermal medium boiler, is provided with main heat in the cavity of this thermal medium boiler and is subjected to hot coil, and this thermal medium boiler housing upper end is provided with the exhaust gases passes that is communicated with desulfation dust-extraction device.
As a preferred embodiment of the present invention, its cavity bottom of described raw materials evaporate jar is provided with evaporation heat release coil pipe, and this evaporation heat release coil pipe is subjected to the hot coil diconnected by superhigh temperature heat carrier pipeloop and described main heat.
As a preferred embodiment of the present invention, its cavity bottom of described raw material preheating jar is provided with pre-exothermic heat coil pipe.
As a preferred embodiment of the present invention, described superhigh temperature heat carrier pipeloop is provided with superhigh temperature heat carrier circulating pump.
As a preferred embodiment of the present invention, described exhaust gases passes is provided with the flue gas heat exchange device, is provided with waste heat in this flue gas heat exchange device and is subjected to hot coil; Described waste heat is subjected to hot coil to pass through the heat carrier pipeloop to be communicated with described pre-exothermic heat coil pipe.
As a preferred embodiment of the present invention, on the described heat carrier pipeloop heat carrier circulating pump is housed.
As a preferred embodiment of the present invention, described preheating material feed-line is provided with the preheating material power delivery unit.
As a preferred embodiment of the present invention, the described feed-line of hot charge again is provided with hot charge power delivery unit again.
Description of drawings:
Fig. 1 is a structural representation of the present invention.
The specific embodiment:
Below in conjunction with drawings and Examples in detail the present invention is described in detail:
A kind of dirty organic materials multi-stage heat exchanger distilling apparatus is referring to accompanying drawing 1; Among the figure: thermal medium boiler 1, main heat is subjected to hot coil 2, superhigh temperature heat carrier circulating pump 3, superhigh temperature heat carrier pipeloop 4, evaporation heat release coil pipe 5, raw materials evaporate jar 6, evaporator discharge vaporization mouth 7, evaporator manhole 8, evaporator feeding mouth 9, one-level condensing heat exchanger 10, raw material preheating jar 11, the hot charge feed-line 12 again, pre-exothermic heat coil pipe 13, preheating can discharge vaporization mouth 14, B-grade condensation heat exchanger 15, preheating can feeding mouth 16, preheating material feed-line 17, raw material storage jar 18, discharge vaporization pipeline 19, liquid phase component collecting tank inlet 20, liquid phase component collecting tank outlet 21, raw material storage jar feeding mouth 22, liquid phase component collecting tank 23, raw material storage jar discharge gate 24, preheating material power delivery unit 25, air-introduced machine 26, desulfurizing dust-collector 27, heat carrier pipeloop 28, heat carrier circulating pump 29, waste heat are subjected to hot coil 30, exhaust gases passes 31, flue gas heat exchange device 32, raw material preheating jar discharge gate 33, the hot charge power delivery unit 34 again.
In the present embodiment, raw materials evaporate jar 6 is placed in the kiln body of bottom fire coal, provide evaporation heat for raw materials evaporate jar 6 by the coal-fired heat release in bottom.
The center upper portion of raw materials evaporate jar 6 is provided with evaporator discharge vaporization mouth 7, and the top avris is respectively arranged with evaporator feeding mouth 9 and the evaporator manhole 8 that inserts appropriate depth.The center upper portion of raw material preheating jar 11 is provided with preheating can discharge vaporization mouth 14, and the top avris is provided with the preheating can feeding mouth 16 that inserts appropriate depth, and the bottom is provided with raw material preheating jar discharge gate 33.Raw material storage jar 18 upper and lowers are respectively arranged with raw material storage jar feeding mouth 22 and raw material storage jar discharge gate 24.The liquid phase component gathering-device is a liquid phase component collecting tank 23, and its top is provided with liquid phase component collecting tank outlet 21.
Raw material storage jars 18 is connected with liquid phase component collecting tank 23, and raw materials evaporate jar 6 is connected with heating combined equipment, and thermal medium boiler 1 is communicated with desulfation dust-extraction device.The evaporator discharge vaporization mouth 7 of raw materials evaporate jar 6 is connected with liquid phase component collecting tank 23 by discharge vaporization pipeline 19; Liquid phase component collecting tank 23 its tops are respectively arranged with the liquid phase component collecting tank inlet 20 and the liquid phase component collecting tank outlet 21 of inserting appropriate depth, are used for the discharge of oiliness waste gas.Raw material storage jar 18 interior raw materials are communicated with raw material preheating jar 11 through the heat exchange cavity of preheating material feed-line 17 and B-grade condensation heat exchanger 15 by its discharge gate 24.
In the present embodiment, heating combined equipment is a thermal medium boiler 1, is provided with main heat in the cavity of thermal medium boiler 1 and is subjected to hot coil 2, and the housing upper end of thermal medium boiler 1 is provided with the exhaust gases passes 31 that is communicated with desulfation dust-extraction device.Exhaust gases passes 31 is provided with flue gas heat exchange device 32, is provided with waste heat in the flue gas heat exchange device 32 and is subjected to hot coil 30; Waste heat is subjected to hot coil 30 by heat carrier pipeloop 28 and pre-exothermic heat coil pipe 13 diconnecteds.Raw materials evaporate jar 6 its cavity bottoms are provided with evaporation heat release coil pipe 5, and evaporation heat release coil pipe 5 is subjected to hot coil 2 diconnecteds by superhigh temperature heat carrier pipeloop 4 and main heat.Pre-exothermic heat coil pipe 13 places the bottom of raw material preheating jar 11 its cavitys.Superhigh temperature heat carrier pipeloop 4 is provided with superhigh temperature heat carrier circulating pump 3.Heat carrier circulating pump 29 is housed on the heat carrier pipeloop 28.Preheating material feed-line 17 is provided with preheating material power delivery unit 25.Raw material preheating jar 11 its discharge gates pass through hot charge feed-line 12 again and are communicated with the evaporator feeding mouth 9 of raw materials evaporate jar 6 through one-level condensing heat exchanger 10.Hot charge feed-line 12 is provided with hot charge power delivery unit 34 more again.
Preheating material power delivery unit 25 has the function that can regulate the raw material conveying capacity; Preheating material power delivery unit 25 is the positive displacement delivery pumps that can regulate material flow.Hot charge power delivery unit 34 has the function that can regulate the raw material conveying capacity again; Hot charge power delivery unit 34 is the positive displacement delivery pumps that can regulate material flow again.
The definition of raw material power delivery unit: every device and method that raw material can be flowed by anticipated orientation is all in the scope of this definition.
Flue gas heat exchange device 32 its structure first-selections are formed by hot coil 30 by flue gas circulation cavity and built-in waste heat; , also can form in specific implementation process as the example explanation at this by other form.
One-level condensing heat exchanger 10 and B-grade condensation heat exchanger 15 its structure first-selections are made up of heat exchange core pipe and heat exchange sandwich shell; , also can form in specific implementation process as the example explanation at this by other form.
To the condensing heat exchanger between the raw material preheating jar 11, be named as one-level condensing heat exchanger 10 by raw materials evaporate jar 6 at this.To the condensing heat exchanger between the raw material storage jar 18, be named as B-grade condensation heat exchanger 15 by raw material preheating jar 11 at this.One-level condensing heat exchanger 10 and B-grade condensation heat exchanger 15 are not limited to form by one, also can form by many.In order to make discharge vaporization media implementation cooling effect better, also can between liquid phase component collecting tank inlet 20, other condenser be installed again at B-grade condensation heat exchanger 15.
Operation principle:
Used oil is injected in the raw material storage jar 18 by raw material storage jar feeding mouth 22.
Enter used oil in the raw material storage jars 18 by a raw material storage jar discharge gate 24, by the heat exchange interlayer of preheating material feed-line 17, enter in the raw material preheating jar 11 by preheating can feeding mouth 16 via preheating material power delivery unit 25, B-grade condensation heat exchanger 15.
Enter used oil in the raw material preheating jar 11 by raw material preheating jar discharge gate 33, via the heat exchange interlayer of hot charge power delivery unit 34, one-level condensing heat exchanger 10 again, enter in the raw materials evaporate jar 6 by evaporator feeding mouth 9 by hot charge feed-line 12 again.
Be about to enter the raw materials evaporate jar 6 of duty and the used oil oil storages in the raw material preheating jar 11 and account for about 0.5 times of tank body capacity greatly, if oil storage is too many, then reduce the gasification expansion space that is heated, used oil liquid phase bubble after will being heated is easily discharged through the discharge vaporization mouth simultaneously with high-temperature oil gas, the oil content quality that obtains by distillation is declined to a great extent, if oil storage very little, may reduce heat exchange area, to operating efficiency is descended, should oil storage be controlled in the relatively reasonable scope according to actual working conditions at this.
Light thermal medium boiler 1, be that main heat is heated by the superhigh temperature heat carrier in the hot coil 2, the superhigh temperature heat carrier after being heated constantly is heated and heat release via superhigh temperature heat carrier circulating pump 3 and evaporation heat release coil pipe 5 diconnecteds and reciprocation cycle by superhigh temperature heat carrier pipeloop 4.
Superhigh temperature flue gas in the thermal medium boiler 1 is preferential to be subjected to hot coil 2 to carry out heat exchange with main heat, through the high-temperature flue gas after the heat exchange under the power of air-introduced machine 26, by exhaust gases passes 31 again with flue gas heat exchange device 32 in waste heat be subjected to hot coil 30 to carry out heat exchange, the flue gas after the heat exchange passes through desulfurizing dust-collector 27 by exhaust gases passes 31 and is discharged into atmosphere via air-introduced machine 26.
Waste heat through the high-temperature flue gas heat exchange constantly is heated and heat release via heat carrier circulating pump 29 and pre-exothermic heat coil pipe 13 diconnecteds and reciprocation cycle by heat carrier pipeloop 28 by the heat carrier in the hot coil 30.
After above-mentioned condition satisfied: the used oil in the raw materials evaporate jar 6 was under the condition of evaporation heat release coil pipe 5 continuous heat releases, the generating gasification Evaporation Phenomenon, entered in the discharge vaporization pipeline 19 by evaporator discharge vaporization mouth 7 by the high-temperature oil gas of steam raising, pass through the heat exchange core pipe of one-level condensing heat exchanger 10 and B-grade condensation heat exchanger 15 respectively, enter in the liquid phase component collecting tank 23 by liquid phase component collecting tank inlet 20, by the high-temperature oil gas of steam raising under the condensing heat-exchange effect of one-level condensing heat exchanger 10 and B-grade condensation heat exchanger 15, the liquefaction that is cooled of most of high-temperature oil gas, the liquid phase component of liquefaction of being cooled is collected by liquid phase component collecting tank 23, and the oiliness waste gas of the liquefaction that wherein can not be condensed on a small quantity is discharged into the external world via liquid phase component collecting tank outlet 21.
Raw material storage jar 18 interior used oil enter in the preheating material feed-line 17 by a raw material storage jar discharge gate 24, under the effect of preheating material power delivery unit 25, heat exchange interlayer via B-grade condensation heat exchanger 15 carries out condensing heat-exchange, and the used oil after the heat exchange enters in the raw material preheating jar 11 by preheating can feeding mouth 16.
After the used oil of heat exchange enters raw material preheating jar 11, continue the continuous preheating of acceptance from the heat carrier loop heating system, used oil after preheating enters in the hot charge feed-line 12 by raw material preheating jar discharge gate 33 again, under the effect of hot charge power delivery unit 34 again, heat exchange interlayer via one-level condensing heat exchanger 10 carries out condensing heat-exchange, and the high temperature used oil after the heat exchange enters in the raw materials evaporate jar 6 by evaporator feeding mouth 9.
In above-mentioned raw materials preheating can 11, accept the used oil of preheating, a spot of steam raising phenomenon will take place, entered in the discharge vaporization pipeline 19 by preheating can discharge vaporization mouth 14 by the high-temperature oil gas of steam raising, pass through the heat exchange core pipe of B-grade condensation heat exchanger 15, enter in the liquid phase component collecting tank 23 by liquid phase component collecting tank inlet 20, by the high-temperature oil gas of steam raising under the condensing heat-exchange effect of B-grade condensation heat exchanger 15, the liquefaction that is cooled of most of high-temperature oil gas, the liquid phase component of liquefaction of being cooled is collected by liquid phase component collecting tank 23, and the oiliness waste gas of the liquefaction that wherein can not be condensed on a small quantity is discharged into the external world via liquid phase component collecting tank outlet 21.
Having constituted at 4 by above-mentioned condition is heated and the integrated system of 3 energy-conservation heat exchange, in order to make this system give full play to best energy-conservation heat exchange effect, can be by strengthening the heat exchange area of one-level condensing heat exchanger 10, the used oil temperature that will come from the B-grade condensation heat exchanger 15 heat exchange interlayers is controlled under the exothermic temperature that is lower than pre-exothermic heat coil pipe 13.
Preheating material power delivery unit 25 has the function of regulating the raw material conveying capacity, is the positive displacement delivery pump that can regulate material flow.Hot charge power delivery unit 34 has the function of regulating the raw material conveying capacity again, is the positive displacement delivery pump that can regulate material flow.These conditions have constituted the Distallation systm of constant material feeding heat exchange continuously.
In order to make this system continue the best operating efficiency of performance, according to system's evaporation capacity, by regulating again the raw material conveying capacity of hot charge power delivery unit 34 and preheating material power delivery unit 25, the relative Sustainable Control of capacity that can make raw materials evaporate jar 6 and raw material preheating jar 11 interior used oil realizes the optimum condition of constant heat exchange, constant evaporation thus in the optimum range that operating mode allows.
In order to understand the capacity of used oil in raw materials evaporate jar 6 and the raw material preheating jar 11, both can calculate by collected liquid phase component, can also observe by liquid level gauge is installed.
When above-mentioned distillation work stopped, operating personnel can be entered in the raw materials evaporate jar 6 by evaporator manhole 8, and the residual residue in distillation back is removed processing.
At distilling used oil:
The superhigh temperature heat carrier can be the embodiment of one of them with " fused salt ", it is the mixture of potassium nitrate (KNO3), natrium nitrosum (NaNO2) and sodium nitrate (NaNO3), its melting temperature is about about 140 ℃, and boiling temperature is higher than 600 ℃, and specific heat is about 0.34.
Heat carrier can be the embodiment of one of them with " conduction oil ".
Claims (10)
1. dirty organic materials multi-stage heat exchanger distilling apparatus, comprise raw material storage jar, the raw material preheating jar, the raw materials evaporate jar, with the raw material tank connected gathering-device of storing in a warehouse, with the tank connected heating combined equipment of raw materials evaporate, the desulfation dust-extraction device that is communicated with heating combined equipment, the floss hole of described raw materials evaporate jar is connected with gathering-device by the discharge vaporization pipeline; It is characterized in that: a described raw material storage jar interior raw material is communicated with the raw material preheating jar through being sleeved on preheating material feed-line and B-grade condensation heat exchanger by its discharge gate.
2. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 1 is characterized in that: described its discharge gate of raw material preheating jar passes through the hot charge feed-line again and is communicated with the feeding mouth of evaporator through first-stage condenser.
3. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 1, it is characterized in that: described heating combined equipment is a thermal medium boiler, be provided with main heat in the cavity of this thermal medium boiler and be subjected to hot coil, this thermal medium boiler housing upper end is provided with the exhaust gases passes that is communicated with desulfation dust-extraction device.
4. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 1, it is characterized in that: its cavity bottom of described raw materials evaporate jar is provided with evaporation heat release coil pipe, and this evaporation heat release coil pipe is subjected to the hot coil diconnected by superhigh temperature heat carrier pipeloop and described main heat.
5. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 1 is characterized in that: its cavity bottom of described raw material preheating jar is provided with pre-exothermic heat coil pipe.
6. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 3 is characterized in that: described superhigh temperature heat carrier pipeloop is provided with superhigh temperature heat carrier circulating pump.
7. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 2, it is characterized in that: described exhaust gases passes is provided with the flue gas heat exchange device, is provided with waste heat in this flue gas heat exchange device and is subjected to hot coil; Described waste heat is subjected to hot coil to pass through the heat carrier pipeloop to be communicated with described pre-exothermic heat coil pipe.
8. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 6 is characterized in that: on the described heat carrier pipeloop heat carrier circulating pump is housed.
9. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 1, it is characterized in that: described preheating material feed-line is provided with the preheating material power delivery unit.
10. dirty organic materials multi-stage heat exchanger distilling apparatus according to claim 8 is characterized in that: the described feed-line of hot charge again is provided with hot charge power delivery unit again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101313404A CN102225239A (en) | 2011-05-20 | 2011-05-20 | Multilevel heat-exchange distilling device for dreggy organic materials |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101313404A CN102225239A (en) | 2011-05-20 | 2011-05-20 | Multilevel heat-exchange distilling device for dreggy organic materials |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102225239A true CN102225239A (en) | 2011-10-26 |
Family
ID=44806259
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101313404A Pending CN102225239A (en) | 2011-05-20 | 2011-05-20 | Multilevel heat-exchange distilling device for dreggy organic materials |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102225239A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102517066A (en) * | 2011-12-10 | 2012-06-27 | 吴国存 | Unbalanced oily waste material high-temperature buffer pyrolysis distillation unit and technology |
| CN108224779A (en) * | 2018-03-18 | 2018-06-29 | 唐山山岛石油化学有限公司 | High condensation point heat carrier heat exchange pipe network device and application method |
| CN109289238A (en) * | 2018-11-16 | 2019-02-01 | 江苏博莱客冷冻科技发展有限公司 | Thermo-compression evaporation crystal system |
| CN112710169A (en) * | 2020-12-07 | 2021-04-27 | 重庆环纽信息科技有限公司 | Waste heat utilization device of waste oil regeneration rectification catalytic system |
| CN112742052A (en) * | 2020-12-09 | 2021-05-04 | 安徽金禾实业股份有限公司 | Continuous distillation equipment of heat sensitive material |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0033849A2 (en) * | 1980-02-06 | 1981-08-19 | BUCKAU - WALTHER Aktiengesellschaft | Method for the recuperation of thermal energy contained in the vapours of multi-step evaporators used in thermal mass-transfer processes, and device for carrying out this method |
| US4371424A (en) * | 1980-07-16 | 1983-02-01 | Sax Zzyzx, Ltd. | Latent heat recirculating system |
| CN1046723A (en) * | 1990-05-11 | 1990-11-07 | 董正耀 | Efficient distilled water production technique and device |
| CN101829434A (en) * | 2010-06-11 | 2010-09-15 | 吴国存 | Convective heat exchange fractionation device |
| CN101858646A (en) * | 2010-06-02 | 2010-10-13 | 吴国存 | Energy-saving and environment-protection heating device for distillation of oily waste materials |
| CN202105448U (en) * | 2011-05-20 | 2012-01-11 | 吴国存 | Multi-stage heat exchange distillation apparatus for dirty organic materials |
-
2011
- 2011-05-20 CN CN2011101313404A patent/CN102225239A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0033849A2 (en) * | 1980-02-06 | 1981-08-19 | BUCKAU - WALTHER Aktiengesellschaft | Method for the recuperation of thermal energy contained in the vapours of multi-step evaporators used in thermal mass-transfer processes, and device for carrying out this method |
| US4371424A (en) * | 1980-07-16 | 1983-02-01 | Sax Zzyzx, Ltd. | Latent heat recirculating system |
| CN1046723A (en) * | 1990-05-11 | 1990-11-07 | 董正耀 | Efficient distilled water production technique and device |
| CN101858646A (en) * | 2010-06-02 | 2010-10-13 | 吴国存 | Energy-saving and environment-protection heating device for distillation of oily waste materials |
| CN101829434A (en) * | 2010-06-11 | 2010-09-15 | 吴国存 | Convective heat exchange fractionation device |
| CN202105448U (en) * | 2011-05-20 | 2012-01-11 | 吴国存 | Multi-stage heat exchange distillation apparatus for dirty organic materials |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102517066A (en) * | 2011-12-10 | 2012-06-27 | 吴国存 | Unbalanced oily waste material high-temperature buffer pyrolysis distillation unit and technology |
| CN102517066B (en) * | 2011-12-10 | 2014-03-26 | 唐山山岛石油化学有限公司 | Unbalanced oily waste material high-temperature buffer pyrolysis distillation unit and technology |
| CN108224779A (en) * | 2018-03-18 | 2018-06-29 | 唐山山岛石油化学有限公司 | High condensation point heat carrier heat exchange pipe network device and application method |
| CN108224779B (en) * | 2018-03-18 | 2024-05-14 | 唐山亿效环保科技有限公司 | High-condensation-point heat carrier heat exchange pipe network device and use method |
| CN109289238A (en) * | 2018-11-16 | 2019-02-01 | 江苏博莱客冷冻科技发展有限公司 | Thermo-compression evaporation crystal system |
| CN112710169A (en) * | 2020-12-07 | 2021-04-27 | 重庆环纽信息科技有限公司 | Waste heat utilization device of waste oil regeneration rectification catalytic system |
| CN112742052A (en) * | 2020-12-09 | 2021-05-04 | 安徽金禾实业股份有限公司 | Continuous distillation equipment of heat sensitive material |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102225239A (en) | Multilevel heat-exchange distilling device for dreggy organic materials | |
| CN104031692B (en) | The device and method of a kind of coking raw gas high temperature direct chilling reparation technology heat medium water | |
| CN102410527A (en) | Composite phase change heat exchanger for flue gas heat recovery of boiler | |
| CN102260583A (en) | Combined process for refining base oil through recycle of waste machine oil | |
| CN113082749A (en) | Treatment method and system for evaporation crystallization and secondary steam purification of fly ash water washing liquid | |
| CN102538199A (en) | Method for absorbing and recycling yellow phosphorus burning heat by using heat-conducting oil | |
| CN104390387B (en) | Double-work medium double circulation refrigeration system | |
| CN101993736B (en) | Method and device for regenerating circular wash oil during rich oil debenzolization of gas purification | |
| CN202105448U (en) | Multi-stage heat exchange distillation apparatus for dirty organic materials | |
| CN102519285B (en) | Integrated technique and special equipment for raw gas waste heat recovery and steam replacement with heat transfer soil | |
| CN101858646B (en) | Energy-saving and environment-protection heating device for distillation of oily waste materials | |
| CN107478067A (en) | Heat recovery system | |
| CN109945174B (en) | Slag flushing water closed circulation utilization system of liquid slag discharging boiler | |
| CN207113635U (en) | Heat recovery system | |
| CN103990372B (en) | The system of ammonia process carbon trapping is carried out in the generating of solar seawater desalination assistant coal | |
| CN103363539B (en) | Comprehensive flue waste heat utilization device | |
| CN111336487A (en) | Coke oven raw gas and waste gas waste heat recycling system | |
| CN201819396U (en) | Energy-saving and environmentally-friendly heating device for distilling oily waste | |
| CN206783619U (en) | A kind of waste heat of coke oven crude gas retracting device | |
| CN203375525U (en) | Comprehensive utilization device of flue waste heat | |
| CN210595933U (en) | Novel coal tar pitch preparation system | |
| CN103292305A (en) | Radial heat tube-ordinary heat exchange tube combined type waste heat recovery device for flue tail gases | |
| CN102425881A (en) | Waste heat utilization method and waste heat utilization system of tail gas in production of carbon black | |
| CN203923120U (en) | The device of the direct chilling reparation technology of a kind of coking raw gas high temperature heat medium water | |
| CN203577362U (en) | Energy-saving type crystallizer used for melamine device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20111026 |