CN100393831C - Distillation process for energy-saving gum rosin - Google Patents
Distillation process for energy-saving gum rosin Download PDFInfo
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- CN100393831C CN100393831C CNB2006101417489A CN200610141748A CN100393831C CN 100393831 C CN100393831 C CN 100393831C CN B2006101417489 A CNB2006101417489 A CN B2006101417489A CN 200610141748 A CN200610141748 A CN 200610141748A CN 100393831 C CN100393831 C CN 100393831C
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- Prior art keywords
- temperature
- steam
- distillation
- still pot
- low
- 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.)
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Links
- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 title claims abstract description 36
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 title claims abstract description 36
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 238000004821 distillation Methods 0.000 title claims description 41
- 238000000034 method Methods 0.000 claims abstract description 27
- 239000007788 liquid Substances 0.000 claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 26
- 239000011347 resin Substances 0.000 claims description 15
- 229920005989 resin Polymers 0.000 claims description 15
- 235000019198 oils Nutrition 0.000 claims description 10
- 238000005086 pumping Methods 0.000 claims description 10
- 235000019476 oil-water mixture Nutrition 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 6
- 230000001698 pyrogenic effect Effects 0.000 claims description 6
- 238000005292 vacuum distillation Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 2
- 239000003245 coal Substances 0.000 abstract description 3
- 239000000498 cooling water Substances 0.000 abstract 1
- 235000005205 Pinus Nutrition 0.000 description 4
- 241000218602 Pinus <genus> Species 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- PZZOEXPDTYIBPI-UHFFFAOYSA-N 2-[[2-(4-hydroxyphenyl)ethylamino]methyl]-3,4-dihydro-2H-naphthalen-1-one Chemical compound C1=CC(O)=CC=C1CCNCC1C(=O)C2=CC=CC=C2CC1 PZZOEXPDTYIBPI-UHFFFAOYSA-N 0.000 description 2
- 235000019687 Lamb Nutrition 0.000 description 2
- 235000008331 Pinus X rigitaeda Nutrition 0.000 description 2
- 235000011613 Pinus brutia Nutrition 0.000 description 2
- 241000018646 Pinus brutia Species 0.000 description 2
- 235000011334 Pinus elliottii Nutrition 0.000 description 2
- 241000142776 Pinus elliottii Species 0.000 description 2
- 235000011609 Pinus massoniana Nutrition 0.000 description 2
- 241000018650 Pinus massoniana Species 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000007639 printing Methods 0.000 description 2
- 238000010079 rubber tapping Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000003248 secreting effect Effects 0.000 description 1
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- Fats And Perfumes (AREA)
Abstract
One kind of energy saving gum rosin distilling process is provided, which features that the closed tail steam and the active tail steam exhausted at the medium and high temperature stages during the gum rosin distilling process are returned to the low temperature stage and the preheating stage of the distilling process separately for reuse. Compared with available gum rosin distilling process, the present invention can shorten the gum rosin distilling time by 50 %, save steam by 50 % and save coal and cooling water obviously.
Description
One, technical field
The invention belongs to the gum resin manufacture field, belong to a kind of technology with vapor distillation gum resin.
Two, background technology
Gum resin is a kind of broad-spectrum raw materials for production, all uses it in a large number at industrial circles such as tire, paint, papermaking, printing, food, clothes, printing and dyeing, furniture, electrical equipment and construction industry.
Gum resin is obtained by the distillation of pine tree excretory rosin.Present rosin both domestic and external factory generally adopts steam to distill processing rosin, it is good that this method has a rosin quality, easy to operate, advantages such as production safety, but heat energy loss is big, reason is that the two stocks another name that consumes in its still-process is the high-temperature steam that closes vapour and working steam, (closing vapour is used for heating rosin liquid but does not contact with rosin liquid, working steam enters rosin liquid Nei And and penetrates the fat liquid layer, being used for extracting out the turps in the fat liquid) both temperature before entering still pot are about about 350 ℃, distill when leaving still pot and finish, tail vapour top temperature separately all can reach about 250 ℃, the tail vapour that closes vapour directly is discharged in the atmosphere, lower the temperature and collect wherein turps and the tail vapour of working steam also will consume a large amount of cold water, hence one can see that in present this distil process, and most heat energy is all invalidly slatterned in the steam.
Three, summary of the invention
Purpose of the present invention: be to utilize closed tail steam and the active tail steam of rosin still-process in hot stage output, its low thermophase and pre-heating stage of returning still-process are utilized again, to save half steam, obtain a kind of new distillation process for energy-saving gum rosin thus.
Distillation process for energy-saving gum rosin of the present invention is realized by following steps:
A, the gum resin still-process just is divided into three lever pieces by temperature, from being preheating section between the original temperature to 130 of fat liquid ℃, the intermediate value of temperature is the low-temperature distillation section when the top temperature of preheating section to distillation finishes, and ends up being the pyrogenic distillation section from the intermediate value to the distillation.Distillation top temperature scope is 180 ℃-200 ℃.
B, the foreheater of fat liquid is set, still pot is set separately in low-temperature distillation section and pyrogenic distillation section at preheating section;
In c, the heat exchanger with first strand of high-temperature steam input high temperature section still pot, make it to become the high temperature section distillation and close vapour, it exports closed tail steam after giving fat liquid with thermal energy transfer.In the jet pipe of closed tail steam at the bottom of by T-valve control input low-temperature zone still pot, become the distillation working steam of low-temperature zone thus, oil pumping is after in the heat exchanger in the T-valve control input foreheater, conduct heat to entering water cooler behind the fat liquid in the foreheater, after water cooler is cooled to oil-water mixture, tell turps and water by water-and-oil separator again, after the foreheater temperature reaches default temperature, promptly control this steam flow and stop to enter foreheater, enter water cooler through bypass by T-valve.When low-temperature zone still pot temperature arrived the temperature of setting, the closed tail steam by the output of T-valve control high temperature section still pot stopped to enter the low-temperature zone still pot, separately discharging.
In d, the jet pipe with second burst of high-temperature steam input high temperature section still pot bottom, make it to become the oil pumping working steam of high temperature section, after the oil pumping, control by T-valve, in the heat exchanger with its tail vapour input low-temperature zone still pot, make it to become the vapour that closes of heating fat liquid, after entering water cooler after the heat transfer and being cooled to oil-water mixture, tell turps and water by water-and-oil separator again; After low-temperature zone still pot temperature arrives predetermined temperature, promptly control this vapour and stop to enter the low-temperature zone still pot, and directly flow to water cooler through bypass by T-valve.
E, after high temperature section still pot temperature reaches outlet temperature and finishes distillation, close all steam, hot rosin in the high temperature section still pot is emitted, put the fat liquid in the low-temperature zone still pot into the high temperature section still pot, fat liquid in the foreheater is put into the low-temperature zone still pot, put new fat liquid into foreheater, be reentered into steam again and repeat the next round distillation procedure.
The used rosin of distillation gum resin of indication of the present invention comprises the rosin of secreting out naturally without tapping from the rosin and the pine tree of trunk tapping with artificial.
Gum resin distil process of the present invention and existing gum resin distil process relatively, can shorten the rosin distillation time half, save steam half, average rosin per ton can be saved the water coolant that coal 60-100kg and saving are equivalent to 2 times of rosin outputs, energy-saving effect is remarkable.
Four, description of drawings
Accompanying drawing is a gum resin distil process schematic flow sheet of the present invention.
A is that vapour is closed in the high temperature section distillation among the figure, and B is a high temperature section distillation working steam, K
1Be foreheater, K
2Be the low-temperature zone still pot, K
3Be the high temperature section still pot, Y
1, Y
2, Y
1, be T-valve, H
1, H
2, H
3Be ball valve, Z
1Be new fat liquid, Z
2Be preheating section fat liquid, Z
3Be low-temperature zone fat liquid, W is a rosin, and J is a turps, and S is a water, and S+J is an oil-water mixture, the 1st, and high temperature section still pot K
3Heat exchanger, the 2nd, low-temperature zone still pot K
2The jet pipe at the end, the 3rd, foreheater K
1Interior heat exchanger, 4 and 9 is water coolers, 5 and 10 is water-and-oil separators, the 6th, close the vapour bypass, the 7th, high temperature section still pot K
3The jet pipe of bottom, the 8th, low-temperature zone still pot K
2Heat exchanger, the 11st, the working steam bypass.
Five, embodiment
Below in conjunction with accompanying drawing gum resin distil process of the present invention is described further.
Referring to accompanying drawing, the gum resin distil process of present embodiment, be that the gum resin still-process just is divided into three lever pieces by temperature, between fat liquid original temperature to 130 ℃ is preheating section, wherein the hot temperature of Pinus massoniana Lamb rosin maximum prefetch is 125 ℃-130 ℃, and slash pine, pinus finlaysoniana, the hot temperature of pinus khasys rosin maximum prefetch are 120 ℃-125 ℃.The intermediate value of temperature is the low-temperature distillation section when the top temperature of preheating section to distillation finishes, and ends up being the pyrogenic distillation section from the intermediate value to the distillation, and distillation top temperature scope is 180 ℃-200 ℃; Wherein the highest distillation temperature of Pinus massoniana Lamb rosin is 195 ℃-200 ℃, and slash pine, pinus finlaysoniana, the highest distillation temperature of pinus khasys rosin are 180 ℃-190 ℃.At preheating section fat liquid foreheater K is set
1, still pot K is set in the low-temperature distillation section
2, still pot K is set separately in the pyrogenic distillation section
3, pot K
2With pot K
1Useful volume is identical, is a pot K
31.2 times to 1.3 times of useful volumes.Pot K
3Heat exchange area be every cubic metre of useful volume 5-6 square metre, the pot K
2The heat exchanger area be every cubic metre of useful volume 6-8 square metre, the pot K
1Heat exchange area be every cubic metre of useful volume 7-9 square metre.
Concrete distillation procedure process is as follows:
A, in the drawings is about 350 ℃ with first burst of temperature, and the high-temperature steam A of pressure 2-4Kg is along arrow input high temperature section still pot K
3Heat exchanger 1 in make it to become that high temperature section is closed Qi ， And and with pot K
3The throttle flow of the speed control steam A that the per minute intensification is 1 ℃ to 1.5 ℃.Steam A exports closed tail steam after giving fat liquid with thermal energy transfer, by T-valve Y
3Control is input low-temperature zone still pot K all
2In the jet pipe 2 at the end, make it to become the working steam of low-temperature zone; After the oil pumping, the low-temperature zone working steam is through T-valve Y
2Control is input foreheater K all
1In the interior heat exchanger 3, conducting heat enters water cooler 4 to behind the fat liquid, after water cooler 4 is cooled to oil-water mixture S+J, tells turps J and water S by water-and-oil separator 5 again; In above-mentioned distillation and warm, T-valve Y
3And Y
3Keep maximum normally open.As foreheater K
1After temperature reaches default temperature, promptly by valve Y
2Control break steam flow direction stops to foreheater K
1Steam supply, steam A enters water cooler 4 by bypass 6 separately; As low-temperature zone still pot K
2When temperature arrives the temperature of setting, by valve Y
3The direction of control break steam flow A stops to pot K
2Steam supply, steam A is disposed in the atmosphere separately.
D, in first gang of steam A input still pot, second burst of temperature is about 350 ℃, pressure is that the high-temperature steam B of 2-4Kg is along arrow input high temperature section still pot K
3In the jet pipe 7 of bottom, make it to become the oil pumping working steam of high temperature section, the throttle flow size of steam B, the oil-water mixture S+J flow that becomes with its oil pumping postcooling is that standard is determined, the S+J flow rate calculation is by pot K
3Every cubic metre of per minute 15-20 of useful volume rises and calculates.After the steam B oil pumping, by T-valve Y
1Low-temperature zone still pot K is all imported in control
2Heat exchanger 8 in, become the vapour that closes of heating fat liquid, after entering water cooler 9 after the heat transfer and being cooled to oil-water mixture S+J, tell turps J and water S by water-and-oil separator 10 again; T-valve Y in above-mentioned still-process
1The normally open that keeps peak flow.As low-temperature zone still pot K
2After temperature arrives predetermined temperature, promptly by valve Y
1Control sub-steam flow and turn to, stop to pot K
2Steam supply, steam B directly flows to water cooler through bypass 11 separately.
E, at high temperature section still pot K
3Temperature reaches outlet temperature finish distillation after, stop to import steam A and B, through valve H
3With high temperature section still pot K
3Interior hot rosin W emits, through valve H
2With low-temperature zone still pot K
2Interior fat liquid Z
3Put still pot K into
3, through valve H
1With foreheater K
1Interior fat liquid Z
2Move on to low-temperature zone still pot K
2Within, with new fat liquid Z
1Put foreheater K into
1In, put into steam A and B more again simultaneously, carry out the next round distillation procedure, whenever defeated the about 20-30 of distillation procedure minute.
By behind the above-mentioned distillation procedure, the rosin distillation time can be shortened half, save half steam, average rosin per ton can be saved the water coolant that the about 60-100kg of coal and saving are equivalent to 2 times of rosin outputs.
Claims (2)
1. distillation process for energy-saving gum rosin is characterized in that: it is that the low thermophase and the pre-heating stage that return still-process utilize again with the closed tail steam and the active tail steam of hot stage discharging in the gum resin still-process, and concrete processing step is:
A, the gum resin still-process is divided into three lever pieces carries out, from being preheating section between the rosin liquid original temperature to 130 ℃, is the low-temperature distillation section from the preheating section top temperature to the intermediate value the still pot top temperature, is the pyrogenic distillation section from intermediate value to top temperature;
B, fat liquid foreheater (K is set at preheating section
1), in the low-temperature distillation section still pot (K is set
2), in the pyrogenic distillation section still pot (K is set
3);
C, with steam (A) input high temperature section still pot (K
3) heat exchanger (1) in become high temperature section steam and close vapour, export closed tail steam after giving fat liquid with thermal energy transfer, closed tail steam is by T-valve (Y
3) control input low-temperature zone still pot (K
2) in the jet pipe (2) at the end, becoming the distillation working steam of low-temperature zone, after the oil pumping, the working steam of low-temperature zone is through T-valve (Y
2) control input foreheater (K
1) in heat exchanger (3) in, enter water cooler (4) after conduct heat giving fat liquid, after water cooler (4) is cooled to oil-water mixture (S+J), tell turps (J) and water (S) by water-and-oil separator (5) again; As foreheater (K
1) after temperature reaches default temperature, promptly by T-valve (Y
2) control stop to foreheater (K
1) steam supply, steam (A) enters water cooler (4) by bypass (6); As low-temperature zone still pot (K
2) when temperature arrives the temperature of setting, by T-valve (Y
3) control stop to its steam supply, steam (A) discharges separately;
D, steam (B) is entered high temperature section still pot (K
3) in the jet pipe (7) of bottom, become the oil pumping working steam of high temperature section, after the oil pumping, by T-valve (Y
1) control, input low-temperature zone still pot (K
2) heat exchanger (8), become the vapour that closes of heating fat liquid, after entering water cooler (9) after the heat transfer and being cooled to oil-water mixture (S+J), tell turps (J) and water (S) by water-and-oil separator (10) again; As low-temperature zone still pot (K
2) after temperature arrives predetermined temperature, promptly by valve (Y
1) stop to its steam supply, steam (B) directly flows to water cooler (9) through bypass (11);
E, at high temperature section still pot (K
3) after temperature reached outlet temperature and finish distillation, steam off (A) and (B) was through ball valve (H
3) with high temperature section still pot (K
3) in hot rosin (W) emit, through valve (H
2) with low-temperature zone still pot (K
2) interior fat liquid (Z
3) put still pot (K into
3), through valve (H
1) with foreheater (K
1) interior fat liquid (Z
2) move on to low-temperature zone still pot (K
2) within, with new fat liquid (Z
1) put foreheater (K into
1) in, be reentered into steam (A) and (B) again, carry out the next round distillation procedure.
2. distillation process for energy-saving gum rosin according to claim 1 is characterized in that described gum resin distillation top temperature scope is 180 ℃-200 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101417489A CN100393831C (en) | 2006-09-30 | 2006-09-30 | Distillation process for energy-saving gum rosin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006101417489A CN100393831C (en) | 2006-09-30 | 2006-09-30 | Distillation process for energy-saving gum rosin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1927974A CN1927974A (en) | 2007-03-14 |
| CN100393831C true CN100393831C (en) | 2008-06-11 |
Family
ID=37858116
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006101417489A Expired - Fee Related CN100393831C (en) | 2006-09-30 | 2006-09-30 | Distillation process for energy-saving gum rosin |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100393831C (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101177589B (en) * | 2007-11-19 | 2011-02-16 | 潘永鑫 | Colophony processing equipment and colophony processing method |
| CN105199607B (en) * | 2015-09-30 | 2017-08-29 | 广西大学 | Lively atmosphere tangential jet self-rotary rosin distilling apparatus and its use |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85102732A (en) * | 1984-04-26 | 1986-10-15 | 新日铁化学株式会社 | The distillating method of styrenic |
| CN2102145U (en) * | 1991-09-13 | 1992-04-22 | 何挺佳 | High-efficiency energy-saving distillation equipment |
| CN2441804Y (en) * | 2000-07-28 | 2001-08-08 | 余国旗 | Serial pot type rosin processing device |
| CN1309578A (en) * | 1998-06-19 | 2001-08-22 | 华盛顿集团国际公司 | Cascade reboiling of ethylbenzene/styrene columns |
| WO2006004962A2 (en) * | 2004-06-30 | 2006-01-12 | Energy Resources Group Llc | Reversible absorption refrigeration |
| CN1817935A (en) * | 2005-01-21 | 2006-08-16 | 拜尔材料科学股份公司 | Formation of uretdione in solution |
-
2006
- 2006-09-30 CN CNB2006101417489A patent/CN100393831C/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85102732A (en) * | 1984-04-26 | 1986-10-15 | 新日铁化学株式会社 | The distillating method of styrenic |
| CN2102145U (en) * | 1991-09-13 | 1992-04-22 | 何挺佳 | High-efficiency energy-saving distillation equipment |
| CN1309578A (en) * | 1998-06-19 | 2001-08-22 | 华盛顿集团国际公司 | Cascade reboiling of ethylbenzene/styrene columns |
| CN2441804Y (en) * | 2000-07-28 | 2001-08-08 | 余国旗 | Serial pot type rosin processing device |
| WO2006004962A2 (en) * | 2004-06-30 | 2006-01-12 | Energy Resources Group Llc | Reversible absorption refrigeration |
| CN1817935A (en) * | 2005-01-21 | 2006-08-16 | 拜尔材料科学股份公司 | Formation of uretdione in solution |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1927974A (en) | 2007-03-14 |
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Owner name: GUANGXI WUZHOU PINE CHEMICALS LTD. Free format text: FORMER OWNER: LU RANGXIAN Effective date: 20110809 |
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| TR01 | Transfer of patent right |
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| EE01 | Entry into force of recordation of patent licensing contract |
Application publication date: 20070314 Assignee: Guangxi Wuzhou City, forestry distillation separation equipment Co. Ltd. Assignor: Lu Rangxian Contract record no.: 2013450000071 Denomination of invention: Distillation process for energy-saving gum rosin Granted publication date: 20080611 License type: Exclusive License Record date: 20130816 |
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Effective date of registration: 20160728 Address after: 343700 Wen Tian Industrial Park, Taihe County, Jiangxi, Ji'an Patentee after: Taihe County feishang forest products Ltd. Address before: 543002 69-3 Fumin road three, the Guangxi Zhuang Autonomous Region, Wuzhou Patentee before: Lu Rangxian |
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