CN106676796A - Supercritical CO2 waterless bleaching device and method for linen coarse yarns - Google Patents
Supercritical CO2 waterless bleaching device and method for linen coarse yarns Download PDFInfo
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- CN106676796A CN106676796A CN201611039618.4A CN201611039618A CN106676796A CN 106676796 A CN106676796 A CN 106676796A CN 201611039618 A CN201611039618 A CN 201611039618A CN 106676796 A CN106676796 A CN 106676796A
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- bleaching
- gas
- kettle
- cosolvent
- liquid
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- 238000004061 bleaching Methods 0.000 title claims abstract description 183
- 238000000034 method Methods 0.000 title claims abstract description 52
- 239000006184 cosolvent Substances 0.000 claims abstract description 75
- 239000012530 fluid Substances 0.000 claims abstract description 55
- 239000007788 liquid Substances 0.000 claims description 89
- 241000208202 Linaceae Species 0.000 claims description 55
- 235000004431 Linum usitatissimum Nutrition 0.000 claims description 55
- 238000003860 storage Methods 0.000 claims description 25
- 239000000203 mixture Substances 0.000 claims description 21
- 239000000945 filler Substances 0.000 claims description 17
- 238000001914 filtration Methods 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 14
- 238000010276 construction Methods 0.000 claims description 11
- 238000011144 upstream manufacturing Methods 0.000 claims description 6
- 239000004793 Polystyrene Substances 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 229920002223 polystyrene Polymers 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000007844 bleaching agent Substances 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- 239000000835 fiber Substances 0.000 abstract description 21
- 238000009987 spinning Methods 0.000 abstract description 8
- 230000004580 weight loss Effects 0.000 abstract description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 abstract description 3
- 238000002156 mixing Methods 0.000 abstract description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 123
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 43
- 239000007789 gas Substances 0.000 description 38
- 239000000243 solution Substances 0.000 description 16
- 239000000047 product Substances 0.000 description 13
- 238000005057 refrigeration Methods 0.000 description 13
- 238000000926 separation method Methods 0.000 description 8
- 239000012535 impurity Substances 0.000 description 7
- 238000009792 diffusion process Methods 0.000 description 6
- 238000004090 dissolution Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000002087 whitening effect Effects 0.000 description 6
- 238000002309 gasification Methods 0.000 description 5
- 238000009834 vaporization Methods 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 229920002488 Hemicellulose Polymers 0.000 description 3
- 235000013351 cheese Nutrition 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 229920005610 lignin Polymers 0.000 description 3
- 239000001814 pectin Substances 0.000 description 3
- 229920001277 pectin Polymers 0.000 description 3
- 235000010987 pectin Nutrition 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 241001649247 Boehmeria Species 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000012736 aqueous medium Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000004043 dyeing Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000012752 auxiliary agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229910001919 chlorite Inorganic materials 0.000 description 1
- 229910052619 chlorite group Inorganic materials 0.000 description 1
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 description 1
- 238000007398 colorimetric assay Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 238000009897 hydrogen peroxide bleaching Methods 0.000 description 1
- 239000002609 medium Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004445 quantitative analysis Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- UKLNMMHNWFDKNT-UHFFFAOYSA-M sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 description 1
- 229960002218 sodium chlorite Drugs 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000000194 supercritical-fluid extraction Methods 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 238000009941 weaving Methods 0.000 description 1
- 238000002166 wet spinning Methods 0.000 description 1
Classifications
-
- D—TEXTILES; PAPER
- D06—TREATMENT OF TEXTILES OR THE LIKE; LAUNDERING; FLEXIBLE MATERIALS NOT OTHERWISE PROVIDED FOR
- D06B—TREATING TEXTILE MATERIALS USING LIQUIDS, GASES OR VAPOURS
- D06B23/00—Component parts, details, or accessories of apparatus or machines, specially adapted for the treating of textile materials, not restricted to a particular kind of apparatus, provided for in groups D06B1/00 - D06B21/00
- D06B23/14—Containers, e.g. vats
- D06B23/18—Sealing arrangements
-
- D—TEXTILES; PAPER
- D06—TREATMENT OF TEXTILES OR THE LIKE; LAUNDERING; FLEXIBLE MATERIALS NOT OTHERWISE PROVIDED FOR
- D06B—TREATING TEXTILE MATERIALS USING LIQUIDS, GASES OR VAPOURS
- D06B23/00—Component parts, details, or accessories of apparatus or machines, specially adapted for the treating of textile materials, not restricted to a particular kind of apparatus, provided for in groups D06B1/00 - D06B21/00
- D06B23/20—Arrangements of apparatus for treating processing-liquids, -gases or -vapours, e.g. purification, filtration, distillation
Abstract
The invention discloses a supercritical CO2 waterless bleaching device and method for linen coarse yarns. On the basis of the prior art, structures of a blending device and a separator are improved, when bleaching is conducted, the linen coarse yarns are placed into a bleaching kettle in sequence, a H2O2 solution serves as a cosolvent, and when a supercritical CO2 state is achieved, bleaching is conducted for 30-150 min on the conditions that the temperature ranges from 50 DEG C to 150 DEG C, the pressure ranges from 8 MPa to 30 MPa, and the CO2 fluid flow rate ranges from 10 g/min to 50 g/min. The whiteness of the linen coarse yarns obtained after bleaching is 40%-75%, the weight loss ratio is 7%-10%, the residual gum content is 7%-12.5%, the single fiber tensile strength is 5-12 cN/dtex, and the elongation at break is 5%-8%. Accordingly, CO2 is utilized for replacing a water medium to achieve clean bleaching production of the linen coarse yarns, the whole process of bleaching is free of pollution and achieves zero emission, and the modern life concepts of fashion bast fiber spinning and green bast fiber spinning are embodied.
Description
Technical field
The present invention relates to a kind of supercritical CO2Liquid waterless bleaching technology, more particularly to a kind of flax roving supercritical CO2
Anhydrous bleaching device and its method for bleaching.
Background technology
Flax fiber is the quality plant fiber that the mankind use earliest, accounts for the 1.5% of natural fiber total amount.Its chemical composition
Mainly include cellulose, hemicellulose, pectin, lignin, waxiness and nitrogen substance etc., wherein hemicellulose, lignin, pectin
It is difficult to remove, and the degree of crystallinity and the degree of orientation of flax fiber molecule are higher, it is easy to ductility, elasticity, convergence to fiber, soft
Soft and crimpiness produces impact, and to flax fiber spinning and weaving process inconvenience is brought.Therefore, flax roving bleaching one
It is directly a difficult problem for bast industry concern.For many years, many research work are all based oneself upon and solve this problem, until the 1950's
Later stage, people just begin one's study flax roving bleaching process, and wet spinning is carried out after rove is bleached, and make accompaniment fully swelling, from
And partial impurities are removed, increase fiber spinnability.The end of the fifties, China successfully have developed flax roving bleaching technology；The seventies
Last flax roving bleaching equipment is substantially perfect.
It is main with water as medium in traditional flax roving bleaching course of processing, sequentially pass through soda boiling, chlorite bleaching, water
Wash, hydrogen peroxide bleaching, water Xian, sour Xian, water Xian's operation, remove hemicellulose in fiber, lignin and pectin, it is final meet spin
To the requirement of flax roving fibre strength and whiteness in yarn operation.Flax roving eliminates part adhesive fine Jing after bleaching
Material between dimension, reduces the contact between fiber, improves the fiber thinness of flax fiber, increased spinning for flax fiber
Property.However, traditional flax roving bleaching process has the shortcomings that water consumption big energy-consuming, technological process length, Financial cost are high.Meanwhile,
After bleaching production, containing auxiliary agents such as substantial amounts of sodium chlorite, soda, hydrogen peroxide in the sewage of discharge, bring seriously to environment
Pollution.
When the temperature and pressure of material under normality is higher than its critical temperature and critical pressure, the material transforms into super
Critical fluids.In the supercritical state, the minor alteration of pressure and temperature, can cause the significant difference of fluid density, and table
It is now the change of fluid dissolubility, so that supercritical fluid has using value.Is held from West Germany Essen in 1978
One " supercritical fluid extraction " international conference rises, and over more than 30 years, supercritical liquid extraction technique is widely used to medicine, changes
The fields such as work, food and environmental protection.Supercritical liquid extraction technique is under conditions of chemical composition is not changed, using shooting flow
The solvability of body and the relation of its density, supercritical fluid are contacted with separate substance so as to selectively that polarity is big
The composition of little, boiling point height and molecular size range is extracted successively, then supercritical fluid is dissolved using temperature and pressure
The impact of ability and realize extract and separate purpose.In conventional material, CO2So that its is nontoxic, harmless, do not fire, it is lazy with chemistry
Property and unique quadrupole moment structure, the features such as critical temperature (31.1 DEG C) and relatively low critical pressure (7.27MPa), become application most
For extensive supercritical fluid.
In order to solve high pollution, the high energy consumption difficult problem of flax roving bleaching process, a kind of flax roving supercritical has been invented
CO2Anhydrous bleaching method.
The content of the invention
In order to solve high pollution, the high energy consumption difficult problem of flax roving bleaching process, the present invention provides a kind of flax roving and surpasses
Critical CO2Anhydrous bleaching device and its method for bleaching, using CO2The bleaching that cleans that aqueous medium realizes flax roving is replaced to give birth to
Produce, for the technology shifts upgrading of bast industry is significant.
A kind of flax roving supercritical CO2Anhydrous bleaching device, including construction unit CO2Storage tank, filter, blender, increasing
Press pump, preheater, heater, bleaching kettle, separating still, cosolvent tank, liquid delivery pump and magnetic force circulating pump, wherein, it is described
CO2Storage tank, filter, blender, booster pump, preheater, bleaching kettle, separating still are sequentially connected with by pipeline, and cosolvent tank leads to
Cross and be connected with above-mentioned blender after pipeline connection liquid delivery pump, the heater is connected by pipeline with bleaching kettle upstream and downstream,
For being heated the material in bleaching kettle；The magnetic force circulating pump is connected by pipeline with bleaching kettle upstream and downstream, for making
Material in bleaching kettle is circulated；Characterized in that,
One. described blender construction unit：
By CO2Entrance, CO2Outlet, cosolvent entrance, cosolvent passage, pin hole conveying tube inlet, pin hole delivery pipe outlet,
Pin hole delivery pipe and gas-liquid hybrid channel constitute；Described gas-liquid mixed passage has the cavity of cylindrical structural, goes to the bottom thereon
Face is uniformly placed with respectively some pin hole delivery pipes, and the pin hole delivery pipe outboard end is connected with the cosolvent passage of oblate cylindricality
Logical, the bottom center on the outside of the direction of the cosolvent passage is provided with cosolvent entrance；The circle of described gas-liquid mixed passage
On the side wall of column construction, CO is symmetrically arranged with2Entrance, CO2Outlet；Described pin hole delivery pipe is on gas-liquid mixed passage
Arrangement mode be, the cross arrangement in the relative position of vertical direction, to keep cosolvent along the uniform of gas-liquid mixed passage
Injection, is capable of achieving CO2With being thoroughly mixed for cosolvent.
Two. described separating still construction unit：
Including cylinder and top cover, the cylinder and top cover are bolted, and on the cylinder gas-liquid mixture is offered
Entrance, liquid outlet and gas outlet I, the gas-liquid mixture entrance is located on cylinder lateral wall, and the liquid outlet is arranged on
Cylinder lower section, the gas outlet I is arranged on cylinder top；Spiral separator, the spiral shell are fixedly connected with the cylinder
Rotating separator from top to bottom includes serpentine pipe, solenoid inlet end and the serpentine pipe port of export, the solenoid inlet end and gas
Liquid mixture entrance is connected, and the serpentine pipe port of export is connected with liquid outlet, in the port of the serpentine pipe port of export
Sealing on wall is provided with filtration sieve plate, and gas outlet II is offered on the serpentine pipe port of export, and the gas outlet II is located at
Between the filtration sieve plate and serpentine pipe.
Specifically, for bleaching system mentioned above, wherein, built with filler, described filler is silicon to the serpentine pipe
Glue or polystyrene, the particle diameter of described filler is 1-10 μm.
Specifically, for bleaching system mentioned above, wherein, the packing material size in the serpentine pipe is from gas-liquid mixture
Entrance to the order of gas outlet II is gradually reduced.
Specifically, for bleaching system mentioned above, wherein, the spiral separator is removably installed in separation
In the cylinder of kettle.
Specifically, for bleaching system mentioned above, wherein, the separating still at least one, each separating still is by pipe
The mode of road series connection connects.
Specifically, for bleaching system mentioned above, wherein, the pin hole delivery pipe in the blender is in gas-liquid mixed
Arrangement mode on passage is, the cross arrangement in the relative position of vertical direction.
Invention additionally discloses a kind of method for bleaching of flax roving, using flax roving supercritical CO mentioned above2Nothing
Water bleaching system is bleached.
Specifically, methods described adopts 30% H2O2Solution is bleach.The conditions of bleaching of the method for bleaching is：It is super
Critical CO2Rate of flow of fluid is 10-50g/min, and bleaching kettle internal temperature is 50-150 DEG C, and pressure is 8-30MPa, and bleaching time is
30-150min。
Unit with identical function in supercritical carbon dioxide fluid anhydrous bleaching equipment of the present invention
Comprising multiple, some booster pumps and heater, some bleaching kettles, some separators are such as may include.People in the art
Member can be configured according to the needs for the treatment of capacity.
Specifically, for bleaching system mentioned above, the separating still by described in two is composed in series multistage by pipeline
Separating still；Have detachable helix tube type separator to increase separating area and big according to the molecule of extract in each separating still
It is little to carry out fine separation successively.
Specifically, for bleaching system mentioned above, composed in parallel by pipeline by two bleaching kettles.
H in cosolvent tank2O2By the cosolvent entrance for injecting blender in the presence of liquid delivery pump, and through altogether
Solvent channel enters pin hole and conveys tube inlet, is flowed out in the outlet of pin hole delivery pipe by pin hole delivery pipe, in gas-liquid mixed passage
Interior and CO2It is sufficiently mixed in the presence of and is injected into inside bleaching kettle, and supercriticality is entered in the presence of preheater.It is molten
Solution has the supercritical CO of cosolvent2Into bleaching kettle, flax roving is placed in bleaching kettle, with H2O2Solution is cosolvent, is reached
To supercritical CO2During state, in temperature 50-150 DEG C, pressure 8-30MPa, CO2Fluid flow 10-50g/min, with this understanding
Flax roving circulation bleaching 30-150min is carried out using magnetic force circulating pump.After bleaching terminates, 3MPa is kept, carry out CO at 30 DEG C2
Fluid recovery, flax roving after being bleached；Flax roving whiteness 40-75% after bleaching, rate of weight loss 7-10%, cull
Rate 7-12.5%, broken filament intensity 5-12cN/dtex, elongation at break 5-8%.The present invention utilizes CO2Replace aqueous medium
Realize flax roving cleans bleaching production, and bleaching overall process is pollution-free, zero-emission, embodies fashion bast fibre spinning, green fiber crops
The modern life theory of spinning.
A kind of described flax roving supercritical CO2Anhydrous bleaching method, technological process is：Flax roving is inserted above
Described supercritical CO2In bleaching kettle；Refrigeration system is opened, works as CO2Pressure of storage tank is down to 4.0MPa, CO2Tank level rises to
400mm, starts to be passed through CO in bleaching kettle2, make CO2Rate of flow of fluid is 10-50g/min；
Specifically, CO2The CO of storage tank output2Fluid, is filtered by filter, inside high-pressure pump injection blender.Help
Cosolvent in solvent tank injects blender via liquid delivery pump.CO2After uniformly mixing in blender with cosolvent, pass through
Booster pump is entered and heated up for the first time in preheater, to increase mixed effect；Subsequently entering heater carries out secondary temperature elevation, to meet drift
Informal voucher part needs.Supercritical CO2Fluid carries cosolvent and enters the two or more bleaching kettles being arranged in parallel, and carries out Caulis et Folium Lini thick
Yarn is bleached.And in the presence of magnetic force circulating pump, drive supercritical CO2Fluid is circulated between bleaching kettle, completes bleaching life
Produce.After the completion of bleaching, the supercritical CO of cosolvent is carried2Fluid is successively in the two or more separating stills being arranged in series
Carry out multiple stage separation, supercritical CO2Gasify as CO2Gas, cosolvent liquefaction is stored in inside separating still for liquid.CO2Gas Jing
After crossing depurator filtration, reclaim enter CO again2Storage tank, to carry out bleaching production next time.Vaporizer is connected with CO2Storage tank and cold
Condenser, to balance CO2Tank inner pressure.
Specifically, CO mentioned above2Technological process with cosolvent in blender is：
H in the cosolvent tank2O2By the cosolvent entrance for injecting blender in the presence of liquid delivery pump, and Jing
Cross cosolvent passage and convey tube inlet into pin hole, flowed out in the outlet of pin hole delivery pipe by pin hole delivery pipe, in gas-liquid mixed
In passage and CO2It is sufficiently mixed in the presence of and is injected into inside bleaching kettle, and supercritical state is entered in the presence of preheater
State.It is dissolved with the supercritical CO of cosolvent2Into bleaching kettle, bleaching kettle internal temperature is made for 50-150 DEG C, pressure is 8-
30MPa, carries out flax roving circulation bleaching using magnetic force circulating pump with this understanding, and bleaching time is 30-150min；Bleaching knot
Shu Hou, keeps 3MPa, carries out CO at 30 DEG C2Fluid recovery, flax roving after being bleached.
Beneficial effects of the present invention are：
1. compared with traditional chemical method for bleaching, spiral separation has been removably secured in separating still of the present invention
Device fills filler to increase separating area according to different grain Jing sizes, furthermore achieved that according to the molecular size of extract
The purpose of fine separation successively is carried out, the pin hole delivery pipe arranged in blender of the present invention is on gas-liquid mixed passage
Arrangement mode is, the cross arrangement in the relative position of vertical direction, to keep cosolvent along the uniform note of gas-liquid mixed passage
Enter, be capable of achieving CO2With being thoroughly mixed for cosolvent.
2. producing one kilogram of Matong using method for bleaching of the present invention often needs CO2Flow 0.1-1kg, needs H2O2Solution 0-
0.2kg, bleaching time needs 30-150min, and flax roving whiteness is 45-75%, the rate of weight loss 5- of rove after bleaching
10%, residual gum content 8-12%, broken filament intensity 6-12cN/dtex, elongation at break 4-7%；Flax roving of the present invention surpasses
Critical CO2Fluid method for bleaching overall process is pollution-free, zero-emission, embodies fashion bast fibre spinning, the modern life theory of green bast fibre spinning.
Description of the drawings
Fig. 1. flax roving supercritical CO2Fluid bleaching process schematic diagram；
1.CO2Storage tank, 2. blender, 3. bleaching kettle, 4. separating still, 5. filter, 6. preheater, 7. liquid delivery pump,
8. cosolvent tank, 9. booster pump, 10. heater, 11. magnetic force circulating pumps；
Fig. 2. blender schematic diagram；
22、CO2Entrance, 23, CO2Outlet, 24, cosolvent entrance, 25, cosolvent passage, 26, pin hole conveying tube inlet,
27th, pin hole delivery pipe outlet, 28, pin hole delivery pipe, 29, gas-liquid mixed passage；
Fig. 3. spiral separator schematic diagram；
41st, cylinder, 42, top cover, 411, gas-liquid mixture entrance, 412, liquid outlet, 413, gas outlet I, 43, spiral
Formula separator, 431, solenoid inlet end, 432, serpentine pipe, 433, the serpentine pipe port of export, 434, filter sieve plate, 435, gas goes out
Mouth II.
Fig. 4. two separating stills are composed in series multiple stage separation kettle by pipeline；
Fig. 5. two bleaching kettles are in parallel by pipeline.
Specific embodiment
Following non-limiting examples can make one of ordinary skill in the art be more fully understood the present invention, but not with
Any mode limits the present invention.
Test method described in following embodiments, if no special instructions, is conventional method；The reagent and material, such as
Without specified otherwise, commercially obtain.
Whiteness of the present invention is according to GB/T 17644-2008《Textile fabric whiteness colorimetric assay method》, residual gum content is according to GB
5889-86《Boehmeria chemical composition quantitative analysis method》Tested；Broken filament intensity, elongation at break are according to GB/
T5886-86《Boehmeria broken filament intensity experiment method》Tested.
Embodiment 1
The specific embodiment of the present invention is described in detail below in conjunction with accompanying drawing.The structure of bleaching kettle used in following embodiments
It is the supercritical carbon dioxide cheese dyeing kettle in the Chinese patent of CN102787459A for publication No., such as in its disclosure
Dyeing caldron structure described in embodiment 1.
A kind of flax roving supercritical CO of the present invention2Bleaching system：
A kind of flax roving supercritical CO2Anhydrous bleaching device, including construction unit CO2Storage tank 1, filter 5, blender
2nd, booster pump 9, preheater 6, heater 10, bleaching kettle 3, separating still 4, cosolvent tank 8, liquid delivery pump 7 and magnetic force circulating pump
11, wherein, described CO2 storage tanks 1, filter 5, blender 2, booster pump 9, preheater 6, bleaching kettle 3, separating still 4 is by pipe
Road is sequentially connected with, and cosolvent tank 8 is connected by pipeline and is connected with above-mentioned blender 2 after liquid delivery pump 7, and the heater 10 leads to
Cross pipeline to connect with the bleaching upstream and downstream of kettle 3, for being heated the material in bleaching kettle 3；The magnetic force circulating pump 11 passes through
Pipeline is connected with the bleaching upstream and downstream of kettle 3, for being circulated the material in bleaching kettle 3；Wherein,
The described construction unit of blender 2：
By CO2Entrance, CO2Outlet, cosolvent entrance, cosolvent passage, pin hole conveying tube inlet, pin hole delivery pipe outlet,
Pin hole delivery pipe and gas-liquid hybrid channel constitute；Described gas-liquid mixed passage has the cavity of cylindrical structural, goes to the bottom thereon
Face is uniformly placed with respectively some pin hole delivery pipes, and the pin hole delivery pipe outboard end is connected with the cosolvent passage of oblate cylindricality
Logical, the bottom center on the outside of the direction of the cosolvent passage is provided with cosolvent entrance；The circle of described gas-liquid mixed passage
On the side wall of column construction, CO is symmetrically arranged with2Entrance, CO2Outlet；Pin hole delivery pipe in the blender 2 is mixed in gas-liquid
Close passage on arrangement mode be, the cross arrangement in the relative position of vertical direction.
Described separating still construction unit：
Including cylinder 41 and top cover 42, the cylinder 41 and top cover 42 are bolted, and offer on the cylinder 41
Gas-liquid mixture entrance 411, liquid outlet 412 and gas outlet I 413, the gas-liquid mixture entrance 411 is located at the side of cylinder 41
On wall, the liquid outlet 412 is arranged on the lower section of cylinder 41, and the gas outlet I 413 is arranged on the top of cylinder 41；The cylinder
Spiral separator 43 is fixedly connected with body 41, the spiral separator 43 from top to bottom includes serpentine pipe 432, serpentine pipe
Arrival end 431 and the serpentine pipe port of export 433, the solenoid inlet end 431 is connected with gas-liquid mixture entrance 411, described
The serpentine pipe port of export 433 is connected with liquid outlet 412, seals on the port inner wall of the serpentine pipe port of export 433 and is provided with
Sieve plate 434 is filtered, gas outlet II 435 is offered on the serpentine pipe port of export 433, the gas outlet II 435 is located at institute
State between filtration sieve plate 434 and serpentine pipe 432.
Built with filler, described filler is silica gel or polystyrene to the serpentine pipe 432, and the particle diameter of described filler is 1-10
μm.Packing material size is gradually reduced from gas-liquid mixture entrance 411 to the order of gas outlet II 435.The spiral separator
43 are removably installed in the cylinder 41 of separating still.
Using the flax roving supercritical CO of said apparatus2Method for bleaching, its bleaching course of work is as follows：
(1) interior circulation bleaching：
First, flax roving bobbin is sequentially connected into female connector to put in bleaching kettle 3, with H2O2Solution is cosolvent, is placed in and helps
In solvent tank 8.
Refrigeration system is opened, when the pressure of CO2 storage tanks 1 is down to 4.0MPa, the liquid level of CO2 storage tanks 1 rises to 400mm, starts to drift
CO is passed through in white kettle 32, make CO2Rate of flow of fluid is 10-50g/min；Liquid CO2Pass through filter 5 when flowing out in CO2 storage tanks 1
Filter, to remove the impurity that may contain.
H in cosolvent tank 82O2Solution injects the cosolvent entrance 24 of blender 2 in the presence of liquid delivery pump 7, and
Pin hole is entered through cosolvent passage 25 and convey tube inlet 26, flowed out in pin hole delivery pipe outlet 27 by pin hole delivery pipe 28.
CO2 enters blender 2 in the presence of high-pressure pump by CO2 entrances 22, and fully mixes with cosolvent in gas-liquid mixed passage 29
Close.Uniform dissolution has the CO of cosolvent2By the CO of blender 22Outlet is flowed out, and supercritical is then entered in the presence of preheater 6
State.It is dissolved with the supercritical CO of cosolvent2Into bleaching kettle 3, the internal temperature of bleaching kettle 3 is made for 50-150 DEG C, pressure is 8-
30MPa, carries out flax roving circulation bleaching using magnetic force circulating pump 11 with this understanding, and bleaching time is 30-150min；Bleaching
After end, 3MPa is kept, carry out CO at 30 DEG C2Fluid recovery, flax roving after being bleached；
(2) supercritical CO2Fluid is flowed in bleaching kettle 3, and permeating to Caulis et Folium Lini cheese disposed thereon from bottom to top is expanded
Flow out after dissipating；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into bleaching kettle 3, and the holding bleaching internal temperature of kettle 3 is
50-150 DEG C, pressure is 8-30MPa, realizes whitening cycle 30-150min using magnetic force circulating pump 11 with this understanding；It is bleached
The thermal loss of journey is compensated by heater 10.Outer circulation is bleached：
Flax roving bobbin is sequentially connected and is nested with bleaching kettle 3, flax roving Jing supercritical COs2Fluid bleaches 20-
After 40min, change fluid traffic direction, now CO2Fluid is entered via the top gas passage of bleaching kettle 3；From top to bottom
Flow out to after Caulis et Folium Lini cheese diffusion disposed thereon；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into drift
White kettle 3, realizes that outer circulation is bleached.
The thermal loss of bleaching process is compensated by heater 10.After bleaching is machined, high-pressure pump and magnetic force are closed
Circulating pump 11.Supercritical CO in the bleaching kettle of kettle 32Fluid enters multiple stage separation kettle 4, separated kettle gas-liquid mixture entrance
411 and the entrance of spiral separator 43 enter separating still in spiral separator 43, in separator interior gradual change type filler
Under effect, keep 3MPa, under the conditions of 20 DEG C so that bleaching product and CO2Gas is kept completely separate；Bleaching product is through different-grain diameter
The filtration arranged in spiral separator 43, spiral separator 43 can be successively flowed out during the filler of size according to molecular size range
Sieve plate 434 may filter that the solid products such as some fibre, improve separating effect.Through the bleaching of the detached liquid of spiral separator 43
Product can pass through to separate the liquid outlet 412 of the bottom of kettle barrel 41 and release, and recycle Jing after being further purified；Through spiral point
Liquid CO after device 432It is converted into gaseous state CO2, gaseous state CO2Flowed out by the gas outlet II 435 of spiral separator 43, and led to
The space separated between kettle barrel 41 and spiral separator 43 is crossed, then is gone out by the gas for being arranged on the top of separation kettle barrel 41
Mouth I 413 flows out separating stills, after filtering again via filter 5, reclaims after condenser refrigeration and enters CO2 storage tanks 1, in case
Next time uses.
Embodiment 2
8kg flax roving bobbins are sequentially connected and are nested with bleaching kettle 3, H2O2Solution is cosolvent, is placed in cosolvent tank
In 8.
In bleaching process, refrigeration system, liquid CO are first turned on2Flow out in CO2 storage tanks 1, filtered by filter 5,
To remove the impurity that may contain.H in cosolvent tank 82O2Solution injects being total to for blender 2 in the presence of liquid delivery pump 7
Colvent inlet, and pin hole conveying tube inlet 26 is entered through cosolvent passage 25, by pin hole delivery pipe 28 in pin hole delivery pipe
Outlet 27 is flowed out, in the gas-liquid mixed passage 29 and CO2It is sufficiently mixed.Uniform dissolution has the CO2 of cosolvent in the work of high-pressure pump
It is injected into under inside bleaching kettle 3；Supercriticality is then entered in the presence of preheater 6.
Supercritical CO2Fluid is through CO2Gas-liquid mixture entrance 411 flow into bleaching kettle 3 in, from bottom to top to Caulis et Folium Lini cylinder
Export after sub- yarn diffusion；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into bleaching kettle 3, keeps bleaching kettle 3
Internal temperature is 80 DEG C, and pressure is 20MPa, CO2Fluid flow 10g/min, is realized with this understanding using magnetic force circulating pump 11
Whitening cycle 60min；The thermal loss of bleaching process is compensated by heater 10.
After bleaching is machined, magnetic force circulating pump 11 is closed.Supercritical CO in the bleaching body of kettle 32Fluid enters many fraction
Helix tube type separator 43 in kettle 4, internally in the presence of gradual change type filler, keeps 3MPa, under the conditions of 20 DEG C so that drift
White product and CO2Gas is kept completely separate；And according to molecular size so that the bleaching product for extracting is successively via helix tube type point
Separate out from device 43 and its filtration sieve plate 434.Extract can be released by separating still bottom liquid outlet 412, gaseous state CO2Then pass through
The gas outlet I 413 of separating still upper end flows out.In the process, the bottom of helix tube type separator 43 is filtered sieve plate 434 and is located at
The bottom of separating still 4, thus form bottom to the CO at top2Gas vaporization passage, it is ensured that the abundant gasification of gas.Gas CO2
Helix tube type separator 43 is flowed out, after filtering again via filter 5, is reclaimed after condenser refrigeration and is entered CO2Storage tank 1,
In case next time uses.
Through supercritical CO2After fluid bleaching, the whiteness 61.5% of flax roving, rate of weight loss 9.3%, residual gum content
10.9%, broken filament intensity 10.8cN/dtex, elongation at break 6.1%.
Embodiment 3
5kg flax roving bobbins are sequentially connected and are nested with bleaching kettle 3, H2O2Solution is cosolvent, is placed in cosolvent tank
In 8.
In bleaching process, refrigeration system, liquid CO are first turned on2In CO2Flow out in storage tank 1, filtered by filter 5, with
The impurity that removal may contain.H in cosolvent tank 82O2Solution injects the common molten of blender 2 in the presence of liquid delivery pump 7
Agent entrance, and pin hole conveying tube inlet 26 is entered through cosolvent passage 25, gone out in pin hole delivery pipe by pin hole delivery pipe 28
Mouth 27 flows out, and is sufficiently mixed with CO2 in gas-liquid mixed passage 29.Uniform dissolution plays the role of the CO2 of cosolvent in high-pressure pump
Under be injected into bleaching kettle 3 inside；Supercriticality is then entered in the presence of preheater 6.
Supercritical CO2Fluid is through CO2Gas-liquid mixture entrance 411 flow into bleaching kettle 3 in, from bottom to top to Caulis et Folium Lini cylinder
Export after sub- yarn diffusion；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into bleaching kettle 3, keeps bleaching kettle 3
Internal temperature is 100 DEG C, and pressure is 15MPa, CO2Fluid flow 20g/min, is realized with this understanding using magnetic force circulating pump 11
Whitening cycle 90min；The thermal loss of bleaching process is compensated by heater 10.
After bleaching is machined, magnetic force circulating pump 11 is closed.Supercritical CO in the bleaching body of kettle 32Fluid enters many fraction
Helix tube type separator 43 in kettle 4, internally in the presence of gradual change type filler, keeps 3MPa, under the conditions of 20 DEG C so that drift
White product and CO2Gas is kept completely separate；And according to molecular size so that the bleaching product for extracting is successively via helix tube type point
Separate out from device 43 and its filtration sieve plate 434.Extract can be released by separating still bottom liquid outlet 412, gaseous state CO2Then pass through
The gas outlet I 413 of separating still upper end flows out.In the process, the bottom of helix tube type separator 43 is filtered sieve plate 434 and is located at
The bottom of separating still 4, thus form bottom to the CO at top2Gas vaporization passage, it is ensured that the abundant gasification of gas.Gas CO2
Helix tube type separator 43 is flowed out, after filtering again via filter 5, is reclaimed after condenser refrigeration and is entered CO2Storage tank 1,
In case next time uses.
Through supercritical CO2After fluid bleaching, the whiteness 58.5% of flax roving, rate of weight loss 8.1%, residual gum content
11.3%, broken filament intensity 12.5cN/dtex, elongation at break 6.3%.
Embodiment 4
10kg flax roving bobbins are sequentially connected and are nested with bleaching kettle 3, H2O2Solution is cosolvent, is placed in cosolvent
In tank 8.
In bleaching process, refrigeration system, liquid CO are first turned on2In CO2Flow out in storage tank 1, filtered by filter 5, with
The impurity that removal may contain.H in cosolvent tank 82O2Solution injects the common molten of blender 2 in the presence of liquid delivery pump 7
Agent entrance, and pin hole conveying tube inlet 26 is entered through cosolvent passage 25, gone out in pin hole delivery pipe by pin hole delivery pipe 28
Mouth 27 flows out, and is sufficiently mixed with CO2 in gas-liquid mixed passage 29.Uniform dissolution plays the role of the CO2 of cosolvent in high-pressure pump
Under be injected into bleaching kettle 3 inside；Supercriticality is then entered in the presence of preheater 6.
Supercritical CO2Fluid is through CO2Gas-liquid mixture entrance 411 flow into bleaching kettle 3 in, from bottom to top to Caulis et Folium Lini cylinder
Export after sub- yarn diffusion；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into bleaching kettle 3, keeps bleaching kettle 3
Internal temperature is 120 DEG C, and pressure is 25MPa, CO2Fluid flow 50g/min, is realized with this understanding using magnetic force circulating pump 11
Whitening cycle 60min；The thermal loss of bleaching process is compensated by heater 10.
After bleaching is machined, magnetic force circulating pump 11 is closed.Supercritical CO in the bleaching body of kettle 32Fluid enters many fraction
Helix tube type separator 43 in kettle 4, internally in the presence of gradual change type filler, keeps 3MPa, under the conditions of 20 DEG C so that drift
White product and CO2Gas is kept completely separate；And according to molecular size so that the bleaching product for extracting is successively via helix tube type point
Separate out from device 43 and its filtration sieve plate 434.Extract can be released by separating still bottom liquid outlet 412, gaseous state CO2Then pass through
The gas outlet I 413 of separating still upper end flows out.In the process, the bottom of helix tube type separator 43 is filtered sieve plate 434 and is located at
The bottom of separating still 4, thus form bottom to the CO at top2Gas vaporization passage, it is ensured that the abundant gasification of gas.Gas CO2
Helix tube type separator 43 is flowed out, after filtering again via filter 5, is reclaimed after condenser refrigeration and is entered CO2Storage tank 1,
In case next time uses.
Through supercritical CO2After fluid bleaching, the whiteness 61.8% of flax roving, rate of weight loss 8.8%, residual gum content
11.5%, broken filament intensity 10.4cN/dtex, elongation at break 7.1%.
Embodiment 5
15kg flax roving bobbins are sequentially connected and are nested with bleaching kettle 3, H2O2Solution is cosolvent, is placed in cosolvent
In tank 8.
In bleaching process, refrigeration system, liquid CO are first turned on2In CO2Flow out in storage tank 1, filtered by filter 5, with
The impurity that removal may contain.H in cosolvent tank 82O2Solution injects the common molten of blender 2 in the presence of liquid delivery pump 7
Agent entrance, and pin hole conveying tube inlet 26 is entered through cosolvent passage 25, gone out in pin hole delivery pipe by pin hole delivery pipe 28
Mouthfuls 27 flow out, in gas-liquid mixed passage 29 and CO2It is sufficiently mixed.Uniform dissolution plays the role of the CO2 of cosolvent in high-pressure pump
Under be injected into bleaching kettle 3 inside；Supercriticality is then entered in the presence of preheater 6.
Supercritical CO2Fluid is through CO2Gas-liquid mixture entrance 411 flow into bleaching kettle 3 in, from bottom to top to Caulis et Folium Lini cylinder
Export after sub- yarn diffusion；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into bleaching kettle 3, keeps bleaching kettle 3
Internal temperature is 150 DEG C, and pressure is 28MPa, CO2Fluid flow 30g/min, is realized with this understanding using magnetic force circulating pump 11
Whitening cycle 150min；The thermal loss of bleaching process is compensated by heater 10.
After bleaching is machined, magnetic force circulating pump 11 is closed.Supercritical CO in the bleaching body of kettle 32Fluid enters many fraction
Helix tube type separator 43 in kettle 4, internally in the presence of gradual change type filler, keeps 3MPa, under the conditions of 20 DEG C so that drift
White product and CO2Gas is kept completely separate；And according to molecular size so that the bleaching product for extracting is successively via helix tube type point
Separate out from device 43 and its filtration sieve plate 434.Extract can be released by separating still bottom liquid outlet 412, gaseous state CO2Then pass through
The gas outlet I 413 of separating still upper end flows out.In the process, the bottom of helix tube type separator 43 is filtered sieve plate 434 and is located at
The bottom of separating still 4, thus form bottom to the CO at top2Gas vaporization passage, it is ensured that the abundant gasification of gas.Gas CO2
Helix tube type separator 43 is flowed out, after filtering again via filter 5, is reclaimed after condenser refrigeration and is entered CO2Storage tank 1,
In case next time uses.
Through supercritical CO2After fluid bleaching, the whiteness 65.6% of flax roving, rate of weight loss 9.2%, residual gum content
10.5%, broken filament intensity 9.8cN/dtex, elongation at break 6.7%.
Embodiment 6
12kg flax roving bobbins are sequentially connected and are nested with bleaching kettle 3, H2O2Solution is cosolvent, is placed in cosolvent
In tank 8.
In bleaching process, refrigeration system, liquid CO are first turned on2In CO2Flow out in storage tank 1, filtered by filter 5, with
The impurity that removal may contain.H in cosolvent tank 82O2Solution injects the common molten of blender 2 in the presence of liquid delivery pump 7
Agent entrance, and pin hole conveying tube inlet 26 is entered through cosolvent passage 25, gone out in pin hole delivery pipe by pin hole delivery pipe 28
Mouth 27 flows out, and is sufficiently mixed with CO2 in gas-liquid mixed passage 29.Uniform dissolution plays the role of the CO2 of cosolvent in high-pressure pump
Under be injected into bleaching kettle 3 inside；Supercriticality is then entered in the presence of preheater 6.
Supercritical CO2Fluid is through CO2Gas-liquid mixture entrance 411 flow into bleaching kettle 3 in, from bottom to top to Caulis et Folium Lini cylinder
Export after sub- yarn diffusion；In the presence of magnetic force circulating pump 11, CO2Fluid is again introduced into bleaching kettle 3, keeps bleaching kettle 3
Internal temperature is 130 DEG C, and pressure is 25MPa, CO2Fluid flow 40g/min, is realized with this understanding using magnetic force circulating pump 11
Whitening cycle 90min；The thermal loss of bleaching process is compensated by heater 10.
After bleaching is machined, magnetic force circulating pump 11 is closed.Supercritical CO in the bleaching body of kettle 32Fluid enters many fraction
Helix tube type separator 43 in kettle 4, internally in the presence of gradual change type filler, keeps 3MPa, under the conditions of 20 DEG C so that drift
White product and CO2Gas is kept completely separate；And according to molecular size so that the bleaching product for extracting is successively via helix tube type point
Separate out from device 43 and its filtration sieve plate 434.Extract can be released by separating still bottom liquid outlet 412, gaseous state CO2Then pass through
The gas outlet I 413 of separating still upper end flows out.In the process, the bottom of helix tube type separator 43 is filtered sieve plate 434 and is located at
The bottom of separating still 4, thus form bottom to the CO at top2Gas vaporization passage, it is ensured that the abundant gasification of gas.Gas CO2
Helix tube type separator 43 is flowed out, after filtering again via filter 5, is reclaimed after condenser refrigeration and is entered CO2Storage tank 1,
In case next time uses.
Through supercritical CO2After fluid bleaching, the whiteness 58.2% of flax roving, rate of weight loss 8.8%, residual gum content
10.8%, broken filament intensity 9.1cN/dtex, elongation at break 5.4%.
Claims (9)
1. a kind of flax roving supercritical CO2Anhydrous bleaching device, including construction unit CO2Storage tank, filter, blender, supercharging
Pump, preheater, heater, bleaching kettle, separating still, cosolvent tank, liquid delivery pump and magnetic force circulating pump, wherein, described CO2
Storage tank, filter, blender, booster pump, preheater, bleaching kettle, separating still are sequentially connected with by pipeline, and cosolvent tank is by pipe
It is connected with above-mentioned blender after road connection liquid delivery pump, the heater is connected by pipeline with bleaching kettle upstream and downstream, is used for
Heated the material in bleaching kettle；The magnetic force circulating pump is connected by pipeline with bleaching kettle upstream and downstream, for making bleaching
Material in kettle is circulated；Characterized in that,
Described blender construction unit：
By CO2Entrance, CO2Outlet, cosolvent entrance, cosolvent passage, pin hole conveying tube inlet, the outlet of pin hole delivery pipe, pin hole
Delivery pipe and gas-liquid hybrid channel constitute；Described gas-liquid mixed passage has the cavity of cylindrical structural, thereon bottom surface point
Some pin hole delivery pipes are not uniformly placed with, the pin hole delivery pipe outboard end is connected with the cosolvent passage of oblate cylindricality,
Bottom center on the outside of the direction of the cosolvent passage is provided with cosolvent entrance；The cylinder of described gas-liquid mixed passage
On the side wall of structure, CO is symmetrically arranged with2Entrance, CO2Outlet；
Described separating still construction unit：
Including cylinder and top cover, the cylinder and top cover are bolted, and gas-liquid mixture entrance is offered on the cylinder,
Liquid outlet and gas outlet I, the gas-liquid mixture entrance is located on cylinder lateral wall, and the liquid outlet is arranged under cylinder
Side, the gas outlet I is arranged on cylinder top；It is fixedly connected with spiral separator in the cylinder, described spiral point
From top to bottom include serpentine pipe, solenoid inlet end and the serpentine pipe port of export, the solenoid inlet end and gas-liquid mixed from device
Thing entrance is connected, and the serpentine pipe port of export is connected with liquid outlet, close on the port inner wall of the serpentine pipe port of export
Envelope is provided with filtration sieve plate, and gas outlet II is offered on the serpentine pipe port of export, and the gas outlet II is located at the mistake
Between screen plate and serpentine pipe.
2. bleaching system according to claim 1, it is characterised in that the serpentine pipe is built with filler, described filler
Silica gel or polystyrene, the particle diameter of described filler is 1-10 μm.
3. bleaching system according to claim 2, it is characterised in that the packing material size in the serpentine pipe is from gas-liquid mixed
Thing entrance to the order of gas outlet II is gradually reduced.
4. bleaching system according to claim 1, it is characterised in that the spiral separator is removably installed in point
In the cylinder of kettle.
5. bleaching system according to claim 1, it is characterised in that the separating still at least one, each separating still passes through
The mode of placed in series connects.
6. bleaching system according to claim 1, it is characterised in that the pin hole delivery pipe in the blender is mixed in gas-liquid
Close passage on arrangement mode be, the cross arrangement in the relative position of vertical direction.
7. a kind of method for bleaching of flax roving, it is characterised in that using claim 1~6 any one described in Caulis et Folium Lini it is thick
Yarn supercritical CO2Anhydrous bleaching device is bleached.
8. method according to claim 7, it is characterised in that methods described using 30% H2O2Solution is bleach.
9. method according to claim 8, it is characterised in that the conditions of bleaching of the method for bleaching is：Supercritical CO2Stream
Rate of flow of fluid is 10-50g/min, and bleaching kettle internal temperature is 50-150 DEG C, and pressure is 8-30MPa, and bleaching time is 30-
150min。
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| CN106676788A (en) * | 2016-11-21 | 2017-05-17 | 大连工业大学 | Flax thick yarn supercritical CO2 biological enzyme scouring device and scouring method thereof |
| CN106835559A (en) * | 2016-11-21 | 2017-06-13 | 大连工业大学 | A kind of flax roving supercritical CO2Biobleaching device and its method for bleaching |
| CN108842342A (en) * | 2018-08-24 | 2018-11-20 | 青岛即发集团股份有限公司 | A method of spun polyester thread is brightened using cylinder yarn non-aqueous dyeing equipment |
| CN113049497A (en) * | 2021-03-12 | 2021-06-29 | 辽宁轻工职业学院 | Supercritical CO of flax roving2Boiling and bleaching self-checking device and method thereof |
| CN114808320A (en) * | 2022-05-20 | 2022-07-29 | 石狮市中纺学服装及配饰产业研究院 | Supercritical fluid anhydrous oil removal and whitening continuous treatment process for polyester products |
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| CN114808320A (en) * | 2022-05-20 | 2022-07-29 | 石狮市中纺学服装及配饰产业研究院 | Supercritical fluid anhydrous oil removal and whitening continuous treatment process for polyester products |
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Effective date of registration: 20211008 Address after: 214237 Yixing Shunchang Linen Textile Co., Ltd., No. 34, Yuanshang Zhenyuan South Road, Xizhu Town, Yixing City, Wuxi City, Jiangsu Province Patentee after: Yixing City Shunshine Linen Textile Co.,Ltd. Address before: 116034 No. 1 light industry garden, Ganjingzi District, Liaoning, Dalian Patentee before: DALIAN POLYTECHNIC University |