GB2311484A - Solvent recovery in dope spinning process - Google Patents
Solvent recovery in dope spinning process Download PDFInfo
- Publication number
- GB2311484A GB2311484A GB9606486A GB9606486A GB2311484A GB 2311484 A GB2311484 A GB 2311484A GB 9606486 A GB9606486 A GB 9606486A GB 9606486 A GB9606486 A GB 9606486A GB 2311484 A GB2311484 A GB 2311484A
- Authority
- GB
- United Kingdom
- Prior art keywords
- gas
- solvent
- gas stream
- spinning
- spinning zone
- 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.)
- Withdrawn
Links
Classifications
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F13/00—Recovery of starting material, waste material or solvents during the manufacture of artificial filaments or the like
- D01F13/02—Recovery of starting material, waste material or solvents during the manufacture of artificial filaments or the like of cellulose, cellulose derivatives or proteins
-
- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F2/00—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof
- D01F2/24—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof from cellulose derivatives
- D01F2/28—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof from cellulose derivatives from organic cellulose esters or ethers, e.g. cellulose acetate
- D01F2/30—Monocomponent artificial filaments or the like of cellulose or cellulose derivatives; Manufacture thereof from cellulose derivatives from organic cellulose esters or ethers, e.g. cellulose acetate by the dry spinning process
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
- Y02P70/62—Manufacturing or production processes characterised by the final manufactured product related technologies for production or treatment of textile or flexible materials or products thereof, including footwear
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Textile Engineering (AREA)
- Spinning Methods And Devices For Manufacturing Artificial Fibers (AREA)
- Artificial Filaments (AREA)
Description
METHOD OF DOPE SPINNING
This invention relates to the spinning of a dope of cellulose ester, and in particular to the recovery of solvent therefrom.
The invention is predominantly concerned with the spinning of cellulose diacetate in the form of a spinning dope comprising a solution in acetone containing a small proportion of water. Such acetate spinning is the conventional process for the production of cellulose filaments for use, inter alia, in cigarette and other filters. However, the invention can also generally relate to any dope spinning process, for example in the preparation of cellulose ester filaments in the textile industry.
In conventional dope spinning, dope is supplied under pressure to a spinneret having a large number of orifices, to produce a series of fine filaments which are dried and further processed as a bundle. The filaments emerging from the spinneret are conventionally passed downwards through a tower in a current of air which generally moves at about the same speed. The air is returned to the atmosphere, but must first be stripped of evaporated solvent, generally acetone. This is conventionally achieved by passing the emerging air through adsorbent or absorbent columns, etc. However, the use of air, particularly in the presence of an adsorbent such as activated carbon having acetone adsorbed thereon, provides a very high risk of explosion. Also, when using air, the acetone concentration should not exceed a certain percentage of the lower explosion limit, thus limiting the concentration of acetone in the drying section. For this reason, the plant must be cited in a hazard zone and must be very carefully controlled.
It is an object of the present invention to overcome the problems of explosion and air pollution by spinning the dope into an inert gas atmosphere and then stripping the acetone from the inert gas by means of condensation.
According to the present invention, therefore, there is provided a method of spinning a cellulose ester dope comprising extruding under pressure a dope containing cellulose ester dissolved in a spinning solvent, into a stream of gas in a spinning zone; separating the spun filaments from the gas stream; recovering solvent from the gas stream; and venting at least some of said gas to the atmosphere; characterised in that the gas is nitrogen or another inert gas which is recycled to the spinning zone, and the solvent recovery includes the steps of:
a) continuously passing at least a portion of the gas stream emerging from the spinning zone through a condensation unit controlled at a predetermined temperature so as to capture a required proportion of solvent from the gas stream; and
b) recirculating the thus-treated gas stream to the spinning zone together with any untreated gas stream.
The condensation unit will, preferably, be one in which the gas stream is brought into direct contact with the chilled solvent and may conveniently comprise a bubble column of chilled solvent cooled by means of a heat exchanger, e.g. a spiral wound tube containing circulating refrigerant, or a spray cooler using chilled solvent, the solvent being chilled by a heat exchanger (e.g. as above) before being sprayed into the solvent vapour - rich gas stream. Other condensation apparatus may be used.
The essence of this invention is the passing of a portion of the gas stream emerging from the spinning zone into the condensation unit. By maintaining the condensation unit at a temperature considerably lower than the temperature of the incoming gas, it is possible to strip a solvent such as acetone from the gas and to return it to the spinning zone with an appropriately low level of remaining solvent. Thus, in brief, the solvent is rather surprisingly removed using acetone itself (and the process can be considered analogous to a method of drying a gas stream by directly contacting it with chilled water).
It is not necessary to treat the entire gas stream, since the gas supplied to the spinning zone should desirably contain a proportion of acetone and water. Indeed, we have found that gas completely stripped of acetone and water gives unsatisfactory results.
In a preferred embodiment of the invention, the bundle of filaments leaving the spinning zone passes through an incoming "rinse" of clean gas, this inflow being the result of an underpressure caused by extraction of a gas flow from the circulating gas flow. The bundle of filaments thus emerges relatively free from acetone and can be subsequently processed as required.
Because a relatively small amount of fresh gas is introduced into the system at this point, it will be clear that an equivalent amount of gas must be removed from the system after the acetone recovery step. Since the main acetone recovery step is operated under conditions which do not remove all the acetone (so that it can be recycled to the spinning zone as explained above) the surplus gas must be further stripped of acetone before venting to the atmosphere. This is simply achieved by a second condensation unit, this time using a very low temperature, typically from -o to -70 C, so as to provide a gas flow to the atmosphere containing, typically, less than 3 kg/h as defined by the German T A Luft regulations.
A preferred embodiment of the invention will now be described with reference to the accompanying figure which comprises a flow chart of the system.
Referring to this chart, a spinning tower A is provided with an input b 1 for dope and an output b2 for a bundle of spun filaments. A fan D1 is connected to another outlet just above the bottom of the spinning tower A to extract gas, thus creating an underpressure at the exit point of the bundle. The tower A is further supplied with an inlet cl for fresh gas to provide a gas lock, the gas and filaments moving in counter current to ensure that acetone is entrained with the emergent gas flow and not with the bundle of filaments.
The fan D1 is arranged to recycle the gas via a heat-exchanger G and a mixer H to the top of the tower A for re-use. A valve V is provided to divert a chosen proportion of the gas stream, typically 5-80, e.g. 20-80% by volume, to a recovery unit El incorporating chilled acetone of which the temperature can be controlled by a heat exchanger (generally using a circulating refrigerant). Means are provided in El to remove the condensed acetone to storage.
Gas emerging from the recovery unit El passes via a fan D2 to be combined with the recirculating, untreated, gas flow to the heat-exchanger G, via run c7.
A take off point above fan D2 allows for surplus gas from the gaslock to be passed through a second recovery unit E2 linked to a secondary acetone return pump F2, the emerging gas being lead to the atmosphere via run c5, typically, at an acetone concentration of about 30 g/m3 An inlet for fresh gas c2 is supplied upstream of fan D1 in order to fill the system during the starting-up procedure. Also, the main exit line from the tower A is provided with an oxygen meter K to check for the presence of any dilution of the inert gas with air.
Claims (13)
1. A method of spinning a cellulose ester dope comprising extruding under pressure a dope containing cellulose ester dissolved in a spinning solvent, into a stream of gas in a spinning zone; separating the spun filaments from the gas stream; recovering the solvent from the gas stream; and venting at least some of said gas to the atmosphere; characterised in that the gas is nitrogen or another inert gas which is recycled to the spinning zone, and the solvent recovery includes the steps of:
a) continuously passing at least a portion of the gas stream emerging from the spinning zone through an condensation unit controlled at a predetermined temperature so as to capture a required proportion of solvent from the gas stream; and
b) recirculating the thus-treated gas stream to the spinning zone together with any untreated gas stream.
2. A method according to Claim 1, in which from 5% to 80% by volume of the gas stream is passed through the condensation unit.
3. A method according to Claim 1 or Claim 2, in which the solvent is maintained at a temperature of from -35 to +40"C.
4. A method according to any of Claims 1 to 3, in which the gas stream passed through the spinning zone is maintained at from 30 to 1300C.
5. A method according to any of Claims 1 to 4, in which the gas stream is pumped out of the spinning zone as the spun filaments exit so as to create an underpressure and a fresh supply of the gas is introduced, thereby providing a gas lock to prevent emergence of solvent-laden gas; and an equivalent quantity of the treated gas emerging from the condensation unit is passed to the atmosphere via a second condensation recovery unit controlled at a predetermined temperature to capture acetone residues to provide the exit gas with an acetone content below the level required by local regulations.
6. A method according to Claim 5, in which the second bath is controlled at a temperature of from 0 to -70 C.
7. A method according to any of Claims I to 6, in which the gas recirculated to the spinning zone contains from 15 to 1500 g solvent per cubic metre.
8. A method according to any of Claims 1 to 6, in which the gas recirculated to the spinning zone contains from 150 to 250 g solvent per cubic metre.
9. A method according to Claim 7, in which the gas recirculated to the spinning zone has a solvent level of from 15 to 25% of that of the gas leaving the spinning zone.
10. A method according to any of the preceding claims in which the condensation unit comprises a bubble column of chilled solvent cooled by a heat exchanger.
11. A method according to any of Claims 1 to 9, in which the condensation unit comprises a spray cooler using solvent chilled by contact with a heat exchanger before being sprayed into the solvent vapour-rich gas stream.
12. A method according to any of Claims 1 to 11, in which the solvent is acetone.
13. A method according to Claim 12, in which the cellulose ester is a diacetate.
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9606486A GB2311484A (en) | 1996-03-27 | 1996-03-27 | Solvent recovery in dope spinning process |
PCT/GB1997/000892 WO1997036030A1 (en) | 1996-03-27 | 1997-03-27 | Method of dope spinning |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB9606486A GB2311484A (en) | 1996-03-27 | 1996-03-27 | Solvent recovery in dope spinning process |
Publications (2)
Publication Number | Publication Date |
---|---|
GB9606486D0 GB9606486D0 (en) | 1996-06-05 |
GB2311484A true GB2311484A (en) | 1997-10-01 |
Family
ID=10791148
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB9606486A Withdrawn GB2311484A (en) | 1996-03-27 | 1996-03-27 | Solvent recovery in dope spinning process |
Country Status (2)
Country | Link |
---|---|
GB (1) | GB2311484A (en) |
WO (1) | WO1997036030A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104711706A (en) * | 2015-03-17 | 2015-06-17 | 中国纺织科学研究院 | Lyocell fiber spinning solution waste recycling device and recycling method thereof |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB238842A (en) * | 1924-08-22 | 1926-05-25 | Rhodiaseta | Process of manufacture of artificial silk and of artificial threads or filaments andapparatus therefor |
GB308564A (en) * | 1928-03-23 | 1929-09-26 | Ruth Aldo Co Inc | Improvements in apparatus for spinning cellulose esters dissolved in volatile solvents |
GB372503A (en) * | 1930-05-07 | 1932-05-12 | Chatillon Italiana Fibre | Dry spinning device for artificial fibres |
GB689407A (en) * | 1949-11-12 | 1953-03-25 | Celanese Corp | Spinning artificial filamentary materials |
GB791784A (en) * | 1955-02-05 | 1958-03-12 | Phrix Werke Ag | Method of recovering the solvent used in the dry-spinning of polyacrylonitrile or copolymers thereof |
GB1172607A (en) * | 1966-11-04 | 1969-12-03 | Toyo Boseki | Dry Spinning Apparatus |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
NL62378C (en) * | 1942-08-25 | |||
US3648436A (en) * | 1970-03-26 | 1972-03-14 | Ingersoll Rand Res Inc | Gasoline vapor recovery |
US3714790A (en) * | 1971-04-13 | 1973-02-06 | Fmc Corp | Apparatus and method for handling volatile liquids |
DE3038790C2 (en) * | 1980-10-14 | 1982-11-25 | Lohmann Gmbh & Co Kg, 5450 Neuwied | Process and system for the recovery of solvents |
US4420317A (en) * | 1981-10-29 | 1983-12-13 | Nelson Stewart | Process for recovering vaporized solvent which eliminates heat exchangers |
JPS6370246A (en) * | 1986-09-11 | 1988-03-30 | Fuji Photo Film Co Ltd | Coating and drying method for band-shaped material |
IT1263743B (en) * | 1993-01-15 | 1996-08-27 | Sapio Produzione Idrogeno Ossi | PLANT FOR THE RECOVERY OF SOLVENTS OR SOLVENT MIXTURES, DISSOLVED IN AIR OR INERT GAS |
-
1996
- 1996-03-27 GB GB9606486A patent/GB2311484A/en not_active Withdrawn
-
1997
- 1997-03-27 WO PCT/GB1997/000892 patent/WO1997036030A1/en active Application Filing
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB238842A (en) * | 1924-08-22 | 1926-05-25 | Rhodiaseta | Process of manufacture of artificial silk and of artificial threads or filaments andapparatus therefor |
GB308564A (en) * | 1928-03-23 | 1929-09-26 | Ruth Aldo Co Inc | Improvements in apparatus for spinning cellulose esters dissolved in volatile solvents |
GB372503A (en) * | 1930-05-07 | 1932-05-12 | Chatillon Italiana Fibre | Dry spinning device for artificial fibres |
GB689407A (en) * | 1949-11-12 | 1953-03-25 | Celanese Corp | Spinning artificial filamentary materials |
GB791784A (en) * | 1955-02-05 | 1958-03-12 | Phrix Werke Ag | Method of recovering the solvent used in the dry-spinning of polyacrylonitrile or copolymers thereof |
GB1172607A (en) * | 1966-11-04 | 1969-12-03 | Toyo Boseki | Dry Spinning Apparatus |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN104711706A (en) * | 2015-03-17 | 2015-06-17 | 中国纺织科学研究院 | Lyocell fiber spinning solution waste recycling device and recycling method thereof |
Also Published As
Publication number | Publication date |
---|---|
WO1997036030A1 (en) | 1997-10-02 |
GB9606486D0 (en) | 1996-06-05 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6699308B1 (en) | Method and apparatus for the drying of natural gas | |
US3726062A (en) | Method of controlling the emission of odors and particulate matter | |
CN103272455A (en) | Device and method for recycling organic solvents from painting waste gas | |
CN101605724A (en) | The recovery method of high-pureness carbon dioxide | |
US20070039469A1 (en) | Method for removing ammonia and dust from a waste gas that results during the production of fertilizers | |
US5190665A (en) | Process and apparatus for removing carbon dioxide and stripping another component from a liquid stream | |
US3616597A (en) | Method for treating and purifying air | |
US20030099585A1 (en) | Method for eliminating traces of mercury in gases | |
US20060057047A1 (en) | Process for removal of so2 from off-gases by reaction with h2o2 | |
DE19645487C1 (en) | Process and device for cleaning gases with heat exchangers | |
EA034961B1 (en) | Removal of dust in urea finishing | |
GB2311484A (en) | Solvent recovery in dope spinning process | |
DE19518797A1 (en) | Process for cleaning inert gases | |
GB881856A (en) | Crimped wet-spun filamentary materials | |
US3248855A (en) | Process for separating carbon dioxide from a gas mixture | |
EP0567607A1 (en) | Process and device for cleaning textiles | |
EP0492135B1 (en) | Device for purification of air with bio filters and process for such a purification of air | |
EP0578629A1 (en) | Process for purification of a flue gas stream by a washing liquid | |
CN204816080U (en) | Printing and dyeing forming machine exhaust treatment device | |
DE2510241A1 (en) | PROCESS FOR THE ABSORPTION OF GASEOUS COMPONENTS FROM GASES | |
DE2318410C3 (en) | Method and device for separating by-products when spinning synthetic fibers | |
JPH0671130A (en) | Apparatus for treating gas containing vapor of water-soluble organic substance | |
US11207634B2 (en) | Apparatus and method for recovering an amine solvent from an acid gas stream | |
CN118594199A (en) | VLA gas recovery processing method and device in acetate fiber production process | |
FR2458306A1 (en) | PROCESS AND INSTALLATION FOR RECOVERING NITROGEN GAS NITROGEN OXIDES |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WAP | Application withdrawn, taken to be withdrawn or refused ** after publication under section 16(1) |