CN1321099C - Process for concentrating lower polyol from thin aqueous solution - Google Patents
Process for concentrating lower polyol from thin aqueous solution Download PDFInfo
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- CN1321099C CN1321099C CNB2005100152700A CN200510015270A CN1321099C CN 1321099 C CN1321099 C CN 1321099C CN B2005100152700 A CNB2005100152700 A CN B2005100152700A CN 200510015270 A CN200510015270 A CN 200510015270A CN 1321099 C CN1321099 C CN 1321099C
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- 238000000034 method Methods 0.000 title claims abstract description 71
- 230000008569 process Effects 0.000 title claims abstract description 53
- 229920005862 polyol Polymers 0.000 title claims abstract description 24
- 150000003077 polyols Chemical class 0.000 title claims abstract description 24
- 239000007864 aqueous solution Substances 0.000 title claims description 3
- 239000000463 material Substances 0.000 claims description 32
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 19
- 238000003672 processing method Methods 0.000 claims description 14
- 241000282326 Felis catus Species 0.000 claims description 12
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 9
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 claims description 6
- DNIAPMSPPWPWGF-UHFFFAOYSA-N propylene glycol Substances CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 claims description 6
- PUPZLCDOIYMWBV-UHFFFAOYSA-N (+/-)-1,3-Butanediol Chemical compound CC(O)CCO PUPZLCDOIYMWBV-UHFFFAOYSA-N 0.000 claims description 4
- 229940058015 1,3-butylene glycol Drugs 0.000 claims description 2
- UXFQFBNBSPQBJW-UHFFFAOYSA-N 2-amino-2-methylpropane-1,3-diol Chemical compound OCC(N)(C)CO UXFQFBNBSPQBJW-UHFFFAOYSA-N 0.000 claims description 2
- BMRWNKZVCUKKSR-UHFFFAOYSA-N butane-1,2-diol Chemical compound CCC(O)CO BMRWNKZVCUKKSR-UHFFFAOYSA-N 0.000 claims description 2
- 235000019437 butane-1,3-diol Nutrition 0.000 claims description 2
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 230000010354 integration Effects 0.000 abstract 1
- 150000005846 sugar alcohols Polymers 0.000 abstract 1
- 239000012141 concentrate Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 230000009467 reduction Effects 0.000 description 7
- 239000004149 tartrazine Substances 0.000 description 6
- 238000000605 extraction Methods 0.000 description 5
- 238000010992 reflux Methods 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 239000004229 Alkannin Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
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- 239000000470 constituent Substances 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000004172 quinoline yellow Substances 0.000 description 3
- 239000002151 riboflavin Substances 0.000 description 3
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- 239000004231 Riboflavin-5-Sodium Phosphate Substances 0.000 description 2
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- 239000002994 raw material Substances 0.000 description 2
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Abstract
The present invention provides a process method for concentrating low-grade polyalcohol from a dilute water solution. A concentration process of the dilute water solution has the steps that 2 to 8 concentration units which are connected in series are used for finishing the whole concentration process; 2 to 6 concentrating towers which are connected in series and are arranged in each concentration unit are used for operation; a polyol concentrated solution is obtained after section concentration of the 2 to 8 concentration units. The whole concentration process can be carried out in a range of vacuum to normal pressure, all of required heat sources are provided by low grade heat sources arranged in a system, and the present invention has good energy saving effect. The present invention also utilizes pressure difference distribution between multi-stage towers which are connected in series and are arranged in each concentration unit. Because of the adoption of a direct connection heat integration heat exchanging structure, the process flow is simple and the operation is stable.
Description
Technical field
The invention belongs to chemical separation technology, particularly a kind of from dilute aqueous soln the processing method of concentrating lower polyol.
Background technology
The production method of dibasic alcohol mainly contains chemical synthesis or fermentation method, and the dibasic alcohol that obtains mostly is dilute aqueous soln, the big energy of thickening process need.
The concentration method of present industrial use mainly is that a unitary plural serial stage concentrates.As shown in Figure 1, dilute aqueous soln concentrates step by step through the tower of plural serial stage, and previous stage tower top outlet steam is given back one-level tower still reboiler heating.Typical operation conditions is:
First step upgrading tower T-101 tower 6.5kg/cm
2The A operation, 157 ℃ of tower top temperatures, 166 ℃ of tower stills;
Second stage upgrading tower T-102 tower 3.0kg/cm
2The A operation, 133 ℃ of tower top temperatures, 140 ℃ of tower stills;
Third stage upgrading tower T-103 tower 1.3kg/cm
2The A operation, 106 ℃ of tower top temperatures, 116 ℃ of tower stills;
Fourth stage upgrading tower T-104 tower 0.15kg/cm
2The A operation, 54 ℃ of tower top temperatures, 87 ℃ of tower stills.
This processing method, adopt a unit plural serial stage to concentrate, the fourth stage concentrates the Tata still will expect the polyvalent alcohol concentrated solution that concentration is higher, the concentration difference variation is inevitable greatly between the adjacent two-stage, cause the higher pressure reduction of hot integrated manipulation require to obtain the integrated required temperature head impellent of heat, cause first step tower still temperature higher.Whole concentration process adopts low-grade heat source to be difficult to realize multistage operations.
In a hot integrated series unit, finish whole concentration process and have following shortcoming:
(1) whole concentration process institute energy requirement provides by first step upgrading tower reboiler, and for large-scale plant, heat-exchange equipment is too huge, and there are certain difficulty in device fabrication and installation, layout.
(2) be subjected to general facilities condition and the system's rerum natura condition restriction can't the integrated operation of more multistage heat, further reduce operation energy consumption.Last step is cooled off water condition to be limited, and can't further reduce working pressure; The first step is subjected to the dibasic alcohol thermal stability limit, should not further improve working pressure.
(3) the integrated temperature difference restriction of being heated, whole concentration process pressure reduction is big, the temperature difference is less, and multitower heat is integrated to be difficult to stable operation.
(4) first step upgrading tower working pressure is higher, and tower still reboiler needs the steam of elevated pressures grade or thermal oil as thermal source, can't utilize the available low-grade heat source of system self.
Summary of the invention
The purpose of this invention is to provide a kind of from dilute aqueous soln the processing method of concentrating lower polyol, can overcome the shortcoming of prior art.This processing method is the efficient hot integrated concentration process of a kind of multistage substep distillatory on the whole.It comprises:
(1) adopts 2～8 upgrading unit serial operations;
(2) each upgrading unit all adopts 2～6 placed in-line towers to realize hot integrated concentration operation;
(3) in each upgrading unit, between previous stage tower and the back one-level tower the integrated interchanger of direct-connected heat is set, be tube side or the shell side that the material of previous stage tower bottom outlet directly enters hot integrated interchanger, the steam of previous stage top of tower outlet is the heating thermal source of conduct back one-level tower directly, enter the shell side or the tube side of hot integrated interchanger, realize the hot integrated operation of adjacent former and later two towers;
(4) in whole concentration process, the cat head operating temperature range is 30～190 ℃, and tower still operating temperature range is 40～200 ℃; Cat head working pressure scope is 0.05～12kg/cm2A.
Said polyvalent alcohol content is 3～30%.
Said dilute aqueous soln is the lower polyol aqueous solution, wherein comprises ethylene glycol, 1,2-propylene glycol, 1 at least, ammediol, 1,2-butyleneglycol, 1,3 butylene glycol, 2, wherein a kind of of 3-butyleneglycol, 1,4-butyleneglycol, glycerol, or comprise above-mentioned two or more lower polyol.
Integrated interchanger tube side of said heat or the heated material of shell side can enter the tower still or the above a certain position of tower still of back one-level tower.
Placed in-line upgrading tower in said each upgrading unit when concentrated accuracy requirement is not high, can adopt flash tank or still or knockout drum to replace placed in-line upgrading tower in said each upgrading unit.
The integrated interchanger of direct-connected heat between the said front and back stages tower can be 1, or adopts 2～3 parallel operations.
Thermal source in the said dilute aqueous soln concentration process is the low-grade steam that adopts the low-grade material steam in the internal system polyvalent alcohol treating process or produced by it, perhaps adopts steam, other thermals source of heat conduction wet goods.
Last unit of said upgrading unit adopts the integrated operation of two towers heat, one tower is operated under condition of normal pressure, the tower still still adopts the heating of internal system low-grade heat source, hot integrated interchanger tube side or the heated material of shell side directly enter the tower still or the above a certain position of tower still of back one-level tower between two towers, and back one-level tower still concentrates a tower still of ultimate density index setting reboiler according to dibasic alcohol.
Provided by the invention from dilute aqueous soln the processing method of concentrating lower polyol, the dilute aqueous soln concentration process is divided into 2～8 placed in-line upgrading units finishes whole concentration process, each upgrading unit inside is again by 2～6 upgrading tower serial operations, the segmentation of 2～8 upgrading units that process is such obtains the polyvalent alcohol concentrated solution after concentrating.The integrated concentration technology of this placed in-line segmentation heat, the scale of the individual equipment that reduces relatively, energy subsection is evenly supplied with, overcome in the ordinary method energy by first step upgrading tower reboiler provide, problems such as equipment is huge, main equipment manufacturing and installation.And because this segmentation concentration technology, except that last upgrading unit, change in concentration between each adjacent concentrated Tata still material of other each upgrading units is all less, therefore the integrated required pressure reduction of heat changes little, making first of each upgrading unit concentrate Tata can adopt than low-grade heat source and heat not high than operation under the low operating pressure, still temperature.For the polyol blend sepn process, the low-grade cat head material steam that the energy of whole concentration process can all be produced by follow-up polyvalent alcohol treating process is supplied with, perhaps produce low-pressure steam and supply with, greatly reduced the operation energy consumption of whole concentration process by low-grade cat head material steam.
The integrated interchanger of this direct-connected heat provided by the invention has simple in structure, is easy to the advantage of stable operation.In the hot integrated technique of common multitower, general previous stage overhead vapours is given back one-level tower still reboiler heating.For the hot integrated technique of four towers shown in the accompanying drawing 1, the heat transfer temperature difference between hot integrated interchanger (E-102, E-103, E-104) tube side and the shell side is lower, causes the tower still reboiler of integrated heat exchange to start difficulty or fluctuation of service easily.The integrated interchanger of direct-connected heat provided by the invention has overcome above-mentioned defective, it relies on the pressure reduction between the front and back stages, temperature, the higher previous stage tower still material of pressure had flashed off a part of gas phase earlier before the integrated heat exchanger entrance of direct-connected heat, temperature of charge reduces simultaneously, then with the integrated heat exchanger shell pass of direct-connected heat in the heat exchange of previous stage overhead vapours, finish the integrated operating process of one-level heat.Because the integrated heat exchanger inlet and outlet of direct-connected heat itself has certain pressure reduction, and previous stage tower still material had contained part gas phase (through the step-down flash distillation) before entering the integrated interchanger of direct-connected heat, therefore do not exist common tower still reboiler to need the problem of preheating section and startup difficulty, become a kind of heat exchange structure of forcing impellent that has, make hot integrated operation more stable.
The whole concentration process of the present invention can carry out in the normal pressure scope in vacuum, and required heating thermal source all can be provided by the internal system low-grade heat source, has obvious energy-saving effect.The present invention also utilizes the pressure reduction between each tower of the inner plural serial stage of each upgrading unit to distribute, and has adopted the integrated heat exchange structure of direct-connected heat, makes that technical process is simpler, operation is more stable.
Description of drawings
Fig. 1 is a kind of typically hot integrated technique flow process of four towers of concentrating lower polyol from dilute aqueous soln.
Fig. 2 be provided by the invention a kind of from dilute aqueous soln the energy-saving technique flow process of concentrating lower polyol.
Fig. 3 be provided by the invention a kind of from dilute aqueous soln the energy-saving technique flow process of concentrating lower polyol.
Embodiment
The invention provides a kind of from dilute aqueous soln the energy-saving process method of concentrating lower polyol, specific embodiments is described in detail as follows with reference to accompanying drawing.
Fig. 1 is a kind of typically hot integrated technique flow process of four towers of concentrating lower polyol from dilute aqueous soln.The dilute aqueous soln raw material is introduced into the first upgrading tower T-101, and T-101 tower still adopts the middle pressure steam heating, and T-101 tower still material removes the second upgrading tower T-102, and the T-101 overhead vapours is given T-102 tower still reboiler E-102 heating.T-102 tower still material removes the 3rd upgrading tower T-103, and the T-102 overhead vapours is given T-103 tower still reboiler E-103 heating.T-103 tower still material removes the 4th upgrading tower T-104, and the T-103 overhead vapours is given T-104 tower still reboiler E-104 heating, and E-105 is the T-104 overhead condenser.Whole dibasic alcohol dilute aqueous soln concentration process adopts level Four (four towers) the hot integrated technique of connecting.
Fig. 2 be provided by the invention a kind of from dilute aqueous soln the energy-saving technique flow process of concentrating lower polyol, whole concentration process is divided into 2 upgrading unit serial operations, first upgrading unit is the integrated operation of three towers heat, and second upgrading unit is the integrated operation of two Tatas heat.
Typical operation conditions is as follows:
T-101 tower 1.1kg/cm
2The A operation, 102 ℃ of tower top temperatures, 108 ℃ of tower stills;
T-102 tower 0.48kg/cm
2The A operation, 80 ℃ of tower top temperatures, 85 ℃ of tower stills;
T-103 tower 0.13kg/cm
2The A operation, 50 ℃ of tower top temperatures, 60 ℃ of tower stills;
T-104 tower 1.0kg/cm
2The A operation, 100 ℃ of tower top temperatures, 110 ℃ of tower stills;
T-105 tower 0.13kg/cm
2The A operation, 50 ℃ of tower top temperatures, 128 ℃ of tower stills.
Polyvalent alcohol concentrated solution after above-mentioned five towers of process concentrate removes the polyvalent alcohol refining system after dewatering, take off the heavy constituent process again.The refining polyvalent alcohol thermostability condition restriction that is subjected to of polyvalent alcohol, the general high-efficient spiral-screen column that adopts under vacuum condition is finished the separation and purification process of polyol blend.Making with extra care with ethylene glycol, propylene glycol is example, the general about 0.15kg/cm of cat head working pressure
2A, about 134～140 ℃ of tower top temperature, about 160 ℃ of tower still temperature.The cat head material steam can produce a large amount of low-pressure steam in this treating process, perhaps can directly provide energy as thermal source for other processes.This part more low-grade energy concentrates at polyvalent alcohol dilute aqueous soln in the past, in the treating process can't focus utilization owing to all need at the bottom of the tower than the higher-grade thermal source.
Fig. 2 provides a kind of from dilute aqueous soln the energy-saving technique flow process of concentrating lower polyol, 2 upgrading unit serial operations, the integrated operation of first upgrading unit three towers heat, the integrated operation of second upgrading unit two Tatas heat.Be described in detail as follows:
Dilute aqueous soln raw material 1 is introduced into the first upgrading tower T-101 of first upgrading unit, the low-pressure steam heating that T-101 tower still reboiler E-101 adopts follow-up polyvalent alcohol FF cat head material steam heating or adopts follow-up polyvalent alcohol FF cat head material to produce.T-101 tower still material 6 removes the integrated interchanger E-102 of direct-connected heat bottom tube side, because T-101 tower 1.1kg/cm
2A operation, T-102 tower 0.48kg/cm
2There is about 0.6kg/cm in the A operation between two towers
2Pressure reduction, after the flash distillation of E-102 bottom pressure relief, pressure is reduced to 0.5kg/cm from T-101 tower still high-temperature material 6 (108 ℃)
2A, temperature are reduced to 86 ℃, and with E-102 shell side T-101 overhead vapours 2 (102 ℃) heat exchange, E-102 tube side outlet material 7 enters the second upgrading tower T-102 tower still then.T-101 overhead vapours lime set 3 parts reflux 5 as the T-101 tower, and another part is as containing 4 extraction of light constituent waste water.
Similar with said process, T-102 overhead vapours 8 enters the integrated interchanger E-103 of direct-connected heat shell side, and T-102 overhead vapours lime set 9 parts reflux 11 as the T-102 tower, and another part is as waste water 10 extraction (not containing light constituent substantially).T-102 tower still material 12 removes the integrated interchanger E-103 of direct-connected heat bottom tube side, and material 13 enters the 3rd upgrading tower T-103 tower still after vacuum flashing, heat exchange.
T-103 overhead vapours 14 is after overhead condenser E-104 condensation, and a part refluxes 16 as the T-103 tower, and another part is as waste water 15 extraction.T-103 tower still material 17 removes second upgrading unit.
T-105 overhead vapours 24 is after overhead condenser E-108 condensation, and a part refluxes 26 as the T-105 tower, and another part is as waste water 25 extraction.T-105 tower still reboiler E-107 adopts the middle pressure steam heating.
Fig. 3 be provided by the invention a kind of from dilute aqueous soln the energy-saving technique flow process of concentrating lower polyol.
Whole concentration process is divided into 3 upgrading unit serial operations, the integrated operation of first and second upgrading unit three towers heat, the integrated operation of the 3rd upgrading unit two Tatas heat.Preceding two upgrading unit operating process are identical with the first upgrading unit operating process shown in Figure 2, and the 3rd upgrading unit operating process is identical with the second upgrading unit operating process shown in Figure 2.The comparative example:
By 100,000 tons of/year dibasic alcohol devices, raw polyol dilute aqueous soln concentration is by 15%, material quantity is by 110 tons of/hour calculating, by provided by the invention from dilute aqueous soln the energy-saving process method of concentrating lower polyol and the integrated concentration technology of common four towers heat contrast, contrast operation's condition and energy-saving effect are as follows:
The integrated concentration technology of common four towers heat as shown in Figure 1, typical operation conditions and operation energy consumption are as follows:
T-101 tower 6.5kg/cm
2The A operation, 157 ℃ of tower top temperatures, 166 ℃ of tower stills;
T-102 tower 3.0kg/cm
2The A operation, 133 ℃ of tower top temperatures, 140 ℃ of tower stills;
T-103 tower 1.3kg/cm
2The A operation, 106 ℃ of tower top temperatures, 116 ℃ of tower stills;
T-104 tower 0.15kg/cm
2The A operation, 54 ℃ of tower top temperatures, 87 ℃ of tower stills.
Whole concentration systems only T-101 tower bottom reboiler E-101 needs the middle pressure steam heating, and the middle pressure steam consumption is: 33 tons/hour.
The typical energy-saving process method that this patent provides as shown in Figure 2, typical operation conditions and operation energy consumption are as follows:
T-101 tower 1.1kg/cm
2The A operation, 102 ℃ of tower top temperatures, 108 ℃ of tower stills;
T-102 tower 0.48kg/cm
2The A operation, 80 ℃ of tower top temperatures, 85 ℃ of tower stills;
T-103 tower 0.13kg/cm
2The A operation, 50 ℃ of tower top temperatures, 60 ℃ of tower stills;
T-104 tower 1.0kg/cm
2The A operation, 100 ℃ of tower top temperatures, 110 ℃ of tower stills;
T-105 tower 0.13kg/cm
2The A operation, 50 ℃ of tower top temperatures, 128 ℃ of tower stills.
Whole concentration systems only T-105 tower bottom reboiler E-107 needs the middle pressure steam heating, and the middle pressure steam consumption is: 4.5 tons/hour.T-101 tower bottom reboiler E-101, the required thermal source of T-104 tower bottom reboiler E-105 are by follow-up polyvalent alcohol FF cat head material steam heating or the low-pressure steam heating of adopting follow-up polyvalent alcohol FF cat head material to produce.
The energy-saving process method of concentrating lower polyol from dilute aqueous soln that this patent provides is compared with the integrated concentration technology of above-mentioned common four towers heat:
Per hour can save middle pressure steam 33-4.5=28.5 ton/hour.
Can save 28.5 tons/hour * 8000 hours/year=228000 tons/year of middle pressure steams every year.
Has distinct economic.
Claims (8)
1, a kind of from dilute aqueous soln the processing method of concentrating lower polyol, it is characterized in that:
(1) adopts 2～8 upgrading unit serial operations;
(2) each upgrading unit all adopts 2～6 placed in-line towers to realize hot integrated concentration operation;
(3) in each upgrading unit, between previous stage tower and the back one-level tower the integrated interchanger of direct-connected heat is set, be tube side or the shell side that the material of previous stage tower bottom outlet directly enters hot integrated interchanger, the steam of previous stage top of tower outlet is the heating thermal source of conduct back one-level tower directly, enter the shell side or the tube side of hot integrated interchanger, realize the hot integrated operation of adjacent former and later two towers;
(4) in whole concentration process, the cat head operating temperature range is 30～190 ℃, and tower still operating temperature range is 40～200 ℃; Cat head working pressure scope is 0.05～12kg/cm
2
2,, it is characterized in that said polyvalent alcohol content is 3～30% according to the said processing method of claim 1.
3, according to the said processing method of claim 1, it is characterized in that said dilute aqueous soln is the lower polyol aqueous solution, wherein comprise ethylene glycol, 1 at least, 2-propylene glycol, 1, ammediol, 1,2-butyleneglycol, 1,3-butyleneglycol, 2, wherein a kind of of 3-butyleneglycol, 1,4-butyleneglycol, glycerol, or comprise above-mentioned two or more lower polyol.
4,, it is characterized in that hot integrated interchanger tube side or the heated material of shell side enter the tower still or the above a certain position of tower still of back one-level tower according to the said processing method of claim 1.
5,, it is characterized in that placed in-line upgrading tower adopts flash tank or still or knockout drum to replace in said each upgrading unit when concentrated accuracy requirement is not high according to the said processing method of claim 1.
6,, it is characterized in that the integrated interchanger of direct-connected heat between the said front and back stages tower is 1, or adopt 2～3 parallel operations according to the said processing method of claim 1.
7,, it is characterized in that the thermal source in the said dilute aqueous soln concentration process is the steam that adopts the low-grade material in the internal system polyvalent alcohol treating process according to the said processing method of claim 1.
8,, it is characterized in that the thermal source in the said dilute aqueous soln concentration process is to adopt steam or thermal oil thermal source according to the said processing method of claim 1.
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| CNB2005100152700A CN1321099C (en) | 2005-09-28 | 2005-09-28 | Process for concentrating lower polyol from thin aqueous solution |
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| CN1321099C true CN1321099C (en) | 2007-06-13 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7850634B2 (en) | 2002-03-04 | 2010-12-14 | Therakos, Inc. | Method for collecting a desired blood component and performing a photopheresis treatment |
| US7914477B2 (en) | 2002-03-04 | 2011-03-29 | Therakos, Inc. | Apparatus for the continuous separation of biological fluids into components and method of using same |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5449841A (en) * | 1993-12-13 | 1995-09-12 | Imperial Chemical Industries Plc | Process for purifying polyols |
| CN1032252C (en) * | 1990-03-30 | 1996-07-10 | 奥林公司 | Process for purifying polyols to remove residues |
| CN1171840C (en) * | 2002-09-25 | 2004-10-20 | 黑龙江省石油化学研究院 | Separation and refining method of 1,3-propylene-glycol |
| CN1183077C (en) * | 1998-09-23 | 2005-01-05 | Basf公司 | Preparation method of high-purity monoethylene glycol |
-
2005
- 2005-09-28 CN CNB2005100152700A patent/CN1321099C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1032252C (en) * | 1990-03-30 | 1996-07-10 | 奥林公司 | Process for purifying polyols to remove residues |
| US5449841A (en) * | 1993-12-13 | 1995-09-12 | Imperial Chemical Industries Plc | Process for purifying polyols |
| CN1183077C (en) * | 1998-09-23 | 2005-01-05 | Basf公司 | Preparation method of high-purity monoethylene glycol |
| CN1171840C (en) * | 2002-09-25 | 2004-10-20 | 黑龙江省石油化学研究院 | Separation and refining method of 1,3-propylene-glycol |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7850634B2 (en) | 2002-03-04 | 2010-12-14 | Therakos, Inc. | Method for collecting a desired blood component and performing a photopheresis treatment |
| US7914477B2 (en) | 2002-03-04 | 2011-03-29 | Therakos, Inc. | Apparatus for the continuous separation of biological fluids into components and method of using same |
| US9238097B2 (en) | 2002-03-04 | 2016-01-19 | Therakos, Inc. | Method for collecting a desired blood component and performing a photopheresis treatment |
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| Publication number | Publication date |
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| CN1765860A (en) | 2006-05-03 |
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