CA1050833A - Optical fiber fabrication involving homogeneous reaction within a moving hot zone - Google Patents
Optical fiber fabrication involving homogeneous reaction within a moving hot zoneInfo
- Publication number
- CA1050833A CA1050833A CA219,629A CA219629A CA1050833A CA 1050833 A CA1050833 A CA 1050833A CA 219629 A CA219629 A CA 219629A CA 1050833 A CA1050833 A CA 1050833A
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- Prior art keywords
- tube
- hot zone
- glass
- temperature
- deposit
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B37/00—Manufacture or treatment of flakes, fibres, or filaments from softened glass, minerals, or slags
- C03B37/01—Manufacture of glass fibres or filaments
- C03B37/012—Manufacture of preforms for drawing fibres or filaments
- C03B37/014—Manufacture of preforms for drawing fibres or filaments made entirely or partially by chemical means, e.g. vapour phase deposition of bulk porous glass either by outside vapour deposition [OVD], or by outside vapour phase oxidation [OVPO] or by vapour axial deposition [VAD]
- C03B37/018—Manufacture of preforms for drawing fibres or filaments made entirely or partially by chemical means, e.g. vapour phase deposition of bulk porous glass either by outside vapour deposition [OVD], or by outside vapour phase oxidation [OVPO] or by vapour axial deposition [VAD] by glass deposition on a glass substrate, e.g. by inside-, modified-, plasma-, or plasma modified- chemical vapour deposition [ICVD, MCVD, PCVD, PMCVD], i.e. by thin layer coating on the inside or outside of a glass tube or on a glass rod
- C03B37/01861—Means for changing or stabilising the diameter or form of tubes or rods
-
- C—CHEMISTRY; METALLURGY
- C03—GLASS; MINERAL OR SLAG WOOL
- C03B—MANUFACTURE, SHAPING, OR SUPPLEMENTARY PROCESSES
- C03B37/00—Manufacture or treatment of flakes, fibres, or filaments from softened glass, minerals, or slags
- C03B37/01—Manufacture of glass fibres or filaments
- C03B37/012—Manufacture of preforms for drawing fibres or filaments
- C03B37/014—Manufacture of preforms for drawing fibres or filaments made entirely or partially by chemical means, e.g. vapour phase deposition of bulk porous glass either by outside vapour deposition [OVD], or by outside vapour phase oxidation [OVPO] or by vapour axial deposition [VAD]
- C03B37/018—Manufacture of preforms for drawing fibres or filaments made entirely or partially by chemical means, e.g. vapour phase deposition of bulk porous glass either by outside vapour deposition [OVD], or by outside vapour phase oxidation [OVPO] or by vapour axial deposition [VAD] by glass deposition on a glass substrate, e.g. by inside-, modified-, plasma-, or plasma modified- chemical vapour deposition [ICVD, MCVD, PCVD, PMCVD], i.e. by thin layer coating on the inside or outside of a glass tube or on a glass rod
-
- G—PHYSICS
- G02—OPTICS
- G02B—OPTICAL ELEMENTS, SYSTEMS OR APPARATUS
- G02B6/00—Light guides; Structural details of arrangements comprising light guides and other optical elements, e.g. couplings
- G02B6/02—Optical fibres with cladding with or without a coating
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Manufacture, Treatment Of Glass Fibers (AREA)
- Glass Compositions (AREA)
Abstract
OPTICAL FIBER FABRICATION AND RESULTING PRODUCT
ABSTRACT OF THE DISCLOSURE
A preform for fabrication of a glass fiber optical transmission line is prepared by chemical reaction of vapor ingredients within a glass tube. Reaction, which may be between chlorides or hydrides of, for example, silicon and germanium with oxygen, occurs preferentially within a constantly traversing hot zone. Flow rates and temperature are sufficient to result in glass formation in the form of particulate matter on the inner surface of the tube. This particulate matter deposits on the tube and is fused with each passage of the hot zone. Continuous rotation of the tube during processing permits attainment of higher tempertures within the heated zone without distortion of the tube.
- i -
ABSTRACT OF THE DISCLOSURE
A preform for fabrication of a glass fiber optical transmission line is prepared by chemical reaction of vapor ingredients within a glass tube. Reaction, which may be between chlorides or hydrides of, for example, silicon and germanium with oxygen, occurs preferentially within a constantly traversing hot zone. Flow rates and temperature are sufficient to result in glass formation in the form of particulate matter on the inner surface of the tube. This particulate matter deposits on the tube and is fused with each passage of the hot zone. Continuous rotation of the tube during processing permits attainment of higher tempertures within the heated zone without distortion of the tube.
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Description
~Q~833 Back~rouncl of the Invention , . .... _ 1. Field of the Inve tlon The invention is concerned with fibers for use as transmission lines in communications systems operating in -the visible or near visible spectra. Such fibers are generally clad for guiding purposes so that refractive index decreases in value from the core center to the periphery either as a step function or as a continuous gradient.
2. Description of the Prior_Art 10"Optical" communications systems, that is systems operating in the visible or near visible spectra, are now at an advanced stage of development. In accordance with the view held by many, commercial use may be expected within a period of about five years.
A system most likely to find initial, and probably long term, use utilizes clad glass fibers as the transmission medium. These fibers, generally having an overall cross-sectional diameter of about 100 ~m, are generally composed `~ of at least two sections: core and cladding. The cladding layer is necessarily of lowered refractive index relative to the core with typical index variation from core to clad being in the range from about 0.01 to 0.05. Structures under study mav be single mode or multimode. The former is characterized by a sufficiently small core section to efficiently accommodate only the first order mode. Such structures may have a core about 1 or 2 ~m. Multimode lines typically have core sections from 50 ~m to 85 or 90 ~m in diameter.
Multimode structures appear to be of somewhat greater interest at this time. The greater core section facilitates splicing and permits more efficient energy :~"
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coupling to source and repeater. Introduction of many modes into or, alternatively, generation o~ many modes within the line does give rise to a dispersion limitation which takes -the form of a smearing due to the differing velocities of different order modes. Mode dispersion effects have been minimized by a continuous focusing structure~ This structure ;
takes -the form of a fiber, the index of which is graded generally exponetially from a high value at the core center.
The fundamental mode which traverses the length of material ~;
is generally confined to the highest index (lowest velocity) region, while higher order modes as path length increases spend longer and longer periods in relatively low index `~
(high velocity) regions.
A number of procedures have been utilized for fabricating clad glass fibers. Most have yielded to procedures which in some way involve vapor source material.
So, typically, chlorides, hydrides, or other compounds of ~ ~ -silica, as well~as desired dopants, tailoring the index, are reacted with oxygen to produce deposits which directly or ultimately serve as glass source material from which the fiber is drawn. Dopant materials include compounds of, for example, boron for lowering index and germanium, titanium, aluminum, and phosphorus for increasing index. Where the ultimate product is to be a graded multimode line, index gradation may be accomplished, for example, by altering the amount or type of dopant during deposition.
- One procedure utilizing vapor source material is chemical vapor deposition (CVD). In this procedure, compounds are passed over a heated surface--e.g., about a rod or within a tube. Temperatures and rates are adjusted so that reaction is solely heterogeneous, i.e., occurs a-t the heated . . ~ . , .. . . .
~C~5~1~33 sur~ace so that the initial material is a continuous glass layer.
An alternative procedure results in -the introduction of such precursor materials into a flame produced by ignition of a gaseous m~xture of, for example, methane and oxygen.
Reaction is, in this instance, homogeneous resulting in formation of glassy particles within the flame. Combustion product and glassy particles then form a moving gas stream which is made incident again on a heated surface, such as -a rod or tube. Adherent particles sometimes called "soot"
are in subsequent processing flushed, and are sintered and fused to result in a glassy layer.
The CVD process has advantages including high purity but suffers from prolonged required deposition periods. Typically, a suitable preform adequate for fabrication of a kilometer of fiber may require periods of a day or longer.
The soot process has the advantage of high speed;
preforms adequate for fabrication of a kilometer of fiber may be prepared in a few hours or less. Disadvantages, however, include at leas-t initial introduction of contaminants, such as solid carbonaceous residue. Since formation takes place within the combustion environment, hydration is inevitable; and this gives rise to the well-known water absorption peaks with their related subharmonics so consequen-tial in various portions of the infrared spectrum.
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Both procedures are now an established part of the art. See, for example, U.S. Patent Nos. 3,711,262, 3,737,~92, and 3,737,293. Modifications in the processes have, to some extent, increased the speed of the CVD process and reduced the effects of contamination ~ hydration in the soot process.
Fibers a kilometer or more in length with losses as low as 2 or
A system most likely to find initial, and probably long term, use utilizes clad glass fibers as the transmission medium. These fibers, generally having an overall cross-sectional diameter of about 100 ~m, are generally composed `~ of at least two sections: core and cladding. The cladding layer is necessarily of lowered refractive index relative to the core with typical index variation from core to clad being in the range from about 0.01 to 0.05. Structures under study mav be single mode or multimode. The former is characterized by a sufficiently small core section to efficiently accommodate only the first order mode. Such structures may have a core about 1 or 2 ~m. Multimode lines typically have core sections from 50 ~m to 85 or 90 ~m in diameter.
Multimode structures appear to be of somewhat greater interest at this time. The greater core section facilitates splicing and permits more efficient energy :~"
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coupling to source and repeater. Introduction of many modes into or, alternatively, generation o~ many modes within the line does give rise to a dispersion limitation which takes -the form of a smearing due to the differing velocities of different order modes. Mode dispersion effects have been minimized by a continuous focusing structure~ This structure ;
takes -the form of a fiber, the index of which is graded generally exponetially from a high value at the core center.
The fundamental mode which traverses the length of material ~;
is generally confined to the highest index (lowest velocity) region, while higher order modes as path length increases spend longer and longer periods in relatively low index `~
(high velocity) regions.
A number of procedures have been utilized for fabricating clad glass fibers. Most have yielded to procedures which in some way involve vapor source material.
So, typically, chlorides, hydrides, or other compounds of ~ ~ -silica, as well~as desired dopants, tailoring the index, are reacted with oxygen to produce deposits which directly or ultimately serve as glass source material from which the fiber is drawn. Dopant materials include compounds of, for example, boron for lowering index and germanium, titanium, aluminum, and phosphorus for increasing index. Where the ultimate product is to be a graded multimode line, index gradation may be accomplished, for example, by altering the amount or type of dopant during deposition.
- One procedure utilizing vapor source material is chemical vapor deposition (CVD). In this procedure, compounds are passed over a heated surface--e.g., about a rod or within a tube. Temperatures and rates are adjusted so that reaction is solely heterogeneous, i.e., occurs a-t the heated . . ~ . , .. . . .
~C~5~1~33 sur~ace so that the initial material is a continuous glass layer.
An alternative procedure results in -the introduction of such precursor materials into a flame produced by ignition of a gaseous m~xture of, for example, methane and oxygen.
Reaction is, in this instance, homogeneous resulting in formation of glassy particles within the flame. Combustion product and glassy particles then form a moving gas stream which is made incident again on a heated surface, such as -a rod or tube. Adherent particles sometimes called "soot"
are in subsequent processing flushed, and are sintered and fused to result in a glassy layer.
The CVD process has advantages including high purity but suffers from prolonged required deposition periods. Typically, a suitable preform adequate for fabrication of a kilometer of fiber may require periods of a day or longer.
The soot process has the advantage of high speed;
preforms adequate for fabrication of a kilometer of fiber may be prepared in a few hours or less. Disadvantages, however, include at leas-t initial introduction of contaminants, such as solid carbonaceous residue. Since formation takes place within the combustion environment, hydration is inevitable; and this gives rise to the well-known water absorption peaks with their related subharmonics so consequen-tial in various portions of the infrared spectrum.
:
~S~3~
Both procedures are now an established part of the art. See, for example, U.S. Patent Nos. 3,711,262, 3,737,~92, and 3,737,293. Modifications in the processes have, to some extent, increased the speed of the CVD process and reduced the effects of contamination ~ hydration in the soot process.
Fibers a kilometer or more in length with losses as low as 2 or
3 dB/kilometer in selected regions of the infrared are now regularly produced in pilot operations.
Summary of the Invention ... . _ According to the invention there is provided ; process for fabrication of a glass fiber optical trans-mission line, comprising a core section and a cladding, wherein the cladding has an index of refraction of a value lower than the maximum index of the core for energy of the wav~length to be transmitted, comprising introducing a moving stream of a vapor mixture including at least one compound glass-forming precursor together with an oxidizing medium into a tube while heating the tube so as to react the said mixture and produce a glassy deposit on the inner surface of the tube, characterized in that heating of tube and contents are by a moving hot zone - produced by a correspondingly moving heat source external to the tube in that combustion within the tube is avo:ided and in that temperature within the hot zone, composition of the vapor mixture, and rate of introduction of the vapor mixture are maintained at values such th~t at least a part of the reaction takes place within the gaseous mixture at a position . .
spaced from the inner walls of the said tube, thereby producing a suspension of oxidic reaction product particulate material, whereby the particulate material while traveling downstream comes to rest on the inner surface of the tube within a xegion which extends from a position within the said hot zone, the moving zone serving the dual functions of: nucleation site for homo-~L(3S~ 33 geneous reac-tion to produce particulate matter; and consolidation site for previously produced particulate matter.
The invention provides for fabrication o~ clad glass fibers by a procedure which combines some of the advantages of the prior art CVD and soot processes.
With usual hea~ing means there is simultaneous he-terogeneous reaction so that a glassy layer is produced within the moving hot zone by reaction at the heated wall surface.
This deposit, which is present under ordinary circu~stances, is identical to the layer produced in the normal CVD processing.
In accordance with the preferred embodiment, the tube within which formation is taking place is continuously rotated about its,own axis. For example, at a speed of 100 rpm, uniformity about the periphery is enhanced. The surface produced by the molten CVD layer may help to hold ~ 4a -~05~33 ~
the "soot" particles d~lring fusion.
~eactant materials include chlorides and hydrides, as well as other compounds which will react with oxygen as ~;
described. ~s in other vapor reaction processes, other gaseous material may be introduced, for example, to act as ;~ carrier or, in the instance of extxemely combustible matter such as hydrides, to act as a diluent.
Continuous fusion within the hot zone and the resultant thickness uniformity of deposit facilitates formation of graded index structures. As in CVD, gradients ~-may be produced by varying reactant composition with the -~
ratio of high index-producing dopant increasing, in this instance, with successive hot zone traversals. Since reaction conditions for different constituents in ~he reactant mix are different, it is possible also to produce a gradient by altering temperature and/or flow rate during processing.
Typical reaction temperatures maintained at least at the tube wall are within the range of from 1200 to 1600 degrees C. These temperatures, high relative to CVD, are responsible for rapidity of preform production. Particularly at the high temperature end of the range, distortion of the usually sillca tube is avoided by rotation. Narrow zones, increased rotation speed, and vertical disposition of the tube may all contribute to the avoidance of tube distortion.
Preforms adequate for preparation of one or a few kilometers of fiber may be prepared during deposition periods of one or a few hours. These preforms are prepared by conventional processing from the deposited product ~o a final configuration which, as presently practiced, may be of ;' . .
- :, . .
MacChesney-O'~onnor 9-4 1~)83;3 1 rod shape with an internal dlame-ter of frorn 4 to fl mm 2 and a length of 18 inches. In usual process-Lng, the tube 3 which served as the deposition substrate becomes the clad.
Summary of the Invention ... . _ According to the invention there is provided ; process for fabrication of a glass fiber optical trans-mission line, comprising a core section and a cladding, wherein the cladding has an index of refraction of a value lower than the maximum index of the core for energy of the wav~length to be transmitted, comprising introducing a moving stream of a vapor mixture including at least one compound glass-forming precursor together with an oxidizing medium into a tube while heating the tube so as to react the said mixture and produce a glassy deposit on the inner surface of the tube, characterized in that heating of tube and contents are by a moving hot zone - produced by a correspondingly moving heat source external to the tube in that combustion within the tube is avo:ided and in that temperature within the hot zone, composition of the vapor mixture, and rate of introduction of the vapor mixture are maintained at values such th~t at least a part of the reaction takes place within the gaseous mixture at a position . .
spaced from the inner walls of the said tube, thereby producing a suspension of oxidic reaction product particulate material, whereby the particulate material while traveling downstream comes to rest on the inner surface of the tube within a xegion which extends from a position within the said hot zone, the moving zone serving the dual functions of: nucleation site for homo-~L(3S~ 33 geneous reac-tion to produce particulate matter; and consolidation site for previously produced particulate matter.
The invention provides for fabrication o~ clad glass fibers by a procedure which combines some of the advantages of the prior art CVD and soot processes.
With usual hea~ing means there is simultaneous he-terogeneous reaction so that a glassy layer is produced within the moving hot zone by reaction at the heated wall surface.
This deposit, which is present under ordinary circu~stances, is identical to the layer produced in the normal CVD processing.
In accordance with the preferred embodiment, the tube within which formation is taking place is continuously rotated about its,own axis. For example, at a speed of 100 rpm, uniformity about the periphery is enhanced. The surface produced by the molten CVD layer may help to hold ~ 4a -~05~33 ~
the "soot" particles d~lring fusion.
~eactant materials include chlorides and hydrides, as well as other compounds which will react with oxygen as ~;
described. ~s in other vapor reaction processes, other gaseous material may be introduced, for example, to act as ;~ carrier or, in the instance of extxemely combustible matter such as hydrides, to act as a diluent.
Continuous fusion within the hot zone and the resultant thickness uniformity of deposit facilitates formation of graded index structures. As in CVD, gradients ~-may be produced by varying reactant composition with the -~
ratio of high index-producing dopant increasing, in this instance, with successive hot zone traversals. Since reaction conditions for different constituents in ~he reactant mix are different, it is possible also to produce a gradient by altering temperature and/or flow rate during processing.
Typical reaction temperatures maintained at least at the tube wall are within the range of from 1200 to 1600 degrees C. These temperatures, high relative to CVD, are responsible for rapidity of preform production. Particularly at the high temperature end of the range, distortion of the usually sillca tube is avoided by rotation. Narrow zones, increased rotation speed, and vertical disposition of the tube may all contribute to the avoidance of tube distortion.
Preforms adequate for preparation of one or a few kilometers of fiber may be prepared during deposition periods of one or a few hours. These preforms are prepared by conventional processing from the deposited product ~o a final configuration which, as presently practiced, may be of ;' . .
- :, . .
MacChesney-O'~onnor 9-4 1~)83;3 1 rod shape with an internal dlame-ter of frorn 4 to fl mm 2 and a length of 18 inches. In usual process-Lng, the tube 3 which served as the deposition substrate becomes the clad.
4 It may, in accordance with the system, be composed of pure silica or of silica which has been doped to alter, generally 6 to reduce its index. Variations may include removal of the 7 tube, as well as deposition of additional material on the 8 outer surface. The tube serving as the substrate during 9 deposition may be retained to serve as a clad, may be removed, or may, during simultaneous deposition, on its 11 outer surface be provided with encompassing layer/s.
12 Brief Description of the Drawing 13 FIG. 1 is a front elevational view of apparatus 14 suitable for practice of the deposi-tion process in accordance with the invention;
16 FIG. 2 is a front elevational view of apparatus ;
17 alternative to that of FIG. l;
18 FIG. 3 is a front elevational view of a section of 19 tubular material depic-ting observed conditions during processing; and 21 FIG. 4, on coordinates of insertion loss in units 22 of dB/kilometer and wavelength in nanome-ters, is a plot 23 showing the relationship of those two parameters for a clad 24 multimode fiber produced in accordance wi-th the invention.
Detailed Description -~
26 1. The Drawing . .
27 FIG. 1 depicts a lathe 1 holding substrate tube 2 28 within which a hot zone is produced by heating means 3 and 29 4 Tube 2 may be rotated, for example, in the direction shown by arrow 5a by means not shown and hot zone is caused 31 to traverse tube 2 by movement of heating means 3 and 32 support 4 as - 6 _ - MacChesney-O'Connor 9-~
1 schematically depicted by double headed arrow 5b, for 2 example, by a threaded feed member 6. ~ gaseous material is 3 introduced into tube 2 via inlet tube 7 which is, in turn, 4 connected to source material reservoirs 8. Such reservoirs may include an oxygen inlet 9 connected to means not shown.
6 As depicted, gaseous material ma~ also be introduced by inlets 7 10 and 11 by means not shown and through in]et 12 from 8 reservoir 13. Reservoirs 14 and 15 contain normally li~uid 9 reactant material which is introduced into tube 2 by means of carrier gas introduced through inlets 10 and 11 with the be;~a 11 arrangement ~ ~ch that the carrier gas is bubbled through 12 such liquids 16 and 17. Exiting material is exhausted -through 13 outlet 18. Not shown is the arrangement of mixing valves 14 and shut off valves which may be utilized to meter ~lows and to make other necessary adjustments in composition. The 16 apparatus of FIG. 1 is generally horizontally disposed. ~ `~
17 The apparatus of FIG. 2 is, in its operational 18 characteristic, quite similar to that o~ FIG. 1. Vertical 19 disposition of the substrate tube, however, lends stability ., .
to the portion of the tube within the hot zone and may 21 permit attainment of higher temperature or o~ longer hot 22 zones in the traversal direction without objectionable 23 dis-tortion. Apparatus depicted includes tube 20 which may .
24 optionally be provided with rotation means not shown. This tube ~s secured to the apparatus by means o~ chucks 21 and 26 22 and a traversing hot zone is produced within tube 20 27 by means of a ring burner 23 which is caused to constantly 28 traverse tube 20 in the direction depicted by double headed 29 arrow 24 by moving means 25. Gaseous material, for example, ~rom source such as 8 o~ FIG. 1 is introduced via inlet 7 ~ -~50833 tube 26 and e~iting material leaves via exhaust 27.
FIG. 3 is a front elevational view o~ a section of a substrate tube 30 as observed during deposition. Depicted is a heating means 31 producing a hot zone 32 which is traversing tube 30 in the direc-tion shown by arrow 33 by means not shown. Gaseous material is introduced at the :Left end of tube 30 and flows in the broken section of the Figure in the direction shown by arrow 34. For the processing conditions, which with respect to traversal direction and hot zone temperature are those of Example l, two regions are clearly observable. Zone 35 downstream of hot zone 32 is filled with a moving powdery suspension of particulate oxidic material, while region 36, devoid of such particulate matter, defines the region within which fusion of deposited material is occurring.
FIG. 4 is a plot for measured loss in uni~s of dB/kilometer as measured on 713 meters of fiber prepared in accordance with an Example herein. Abscissa units are wavelength in nanometers. It is seen that loss is at a minimum of about 2 dB/kilometer for the wavelength range of about 1060 to 1100 nm (the limiting value on the plot). The peak at about 950 nm, as well as those at 880 and 730 nm, are characteristic sub-harmonics of the fundamental water absorption.
2. Processing Re~uirements -a. Reaction Temperature Superficially, the inventive technique resembles conventional chemical vapor deposition. However, whereas CVD conditions are so arranged that deposition is solely the result of heterogeneous formation at a heated substrate surface, procedures of this invention rely upon significaht .
, ``~ ` 1(3154C~833 homogeneous reaction. In generalj 50 percent or more of reaction product is produced in a position removed from substrate surface and results in the formation of solid~
oxidic particles of the desired glass composition. These particles are similar to -those produced during the "soot"
process.
Homogeneous reaction is the result of sufficient rate of reactant introduction and sufficient reaction temperature. Such conditlons may be achieved simply by increasing one or both parameters until homogeneous reaction i9 visually observed. To optimize the process from the ~ ;~
standpoint of reaction, high temperatures are utilized. For `~
the usual silica based systems which comprise the preferred embodiment, temperatures at least at the substrate wall are ; generally maintained at a minimum oE 1200 degrees C at the moving position corresponding with the hot 20ne. Maximum a ` : :~
tempe ~ ures are ultimately limited by significant wall distortion. For horizontally disposed apparatus, ~uch as ~ that shown in FIG. 1, in which a hot zone of the length of ~ 20 approximately 2 cm moves at the!rate of about 45 cm/min within a tube rotated at the rate of about 100 rpm~ a temperature of 1600 degrees C may be produced without ~;
harmful tube distortion. Decreasing the length of the hot , . ~
zone, increasing the rate of rotation, increasing reactant flow rate, vertical disposition of the tube, are all factors .,:: .
which may permit use of higher maximum temperatures without ;~
variation in tube geometry. Indicated temperatures are those measured by means of an optical pyrometer focused at the outer tube surface. It has been estimated that for :
typical conditions the thermal gradient across the tube may be as high as 300 degrees C.
:
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.
: ,, . . . ~ , .
b. Flow Rates This parameter, like temperature, is dependen-t upon other processing conditions. Again, a ~inimum accep-table rate for those purposes may be determined by visual observation.
~ighest flow rates are ~or those materials which by virtue of combustibility, high vapor pressure, etc., are diluted to a signiEicant extent by inert material. Examples are the hydrides where dilution frequently is as high as 99.5 volume percent based on the total reactant content may necessitate a linear flow rate of at least 1 m~ter per second. Chlorides, ;
which do not present this problem, need not be diluted to avoid combustion. Inert material, such as nitrogen or helium, is introduced solely for transfer purposes and need b~ present only in amount typically of up to 10 percent by volume.
Flow rates are, as indicated, temperature dependent, with the required homogeneous reaction taking place at acceptable rate only by an increase flow of about 50 percent for each hundred degree increase in reaction temperature.
c. Reactants Examples were carried out using chlorides and hydrides. Other gaseous materials of sufficient vapor pressure under processing conditions preferably which react with oxygen or oxygen bearing material to produce the required oxidic glass may be subs'cituted. In a typical system, the substrate tube is silica-~generally undoped. Where this -~ tube is of ordinary purity, first reactant introduced may be such as to result in the formation of a flrst layer of undoped silica or doped with an oxide such as B2O3 which serves to lower the refractive index, which acts as a part of the clad and presents a barrier to diffusing impurlty -10- . ~
~50~333 from the tube. It may be considered that, under these - circumstances, the substrate tube ultimately serves as a mechanical support rather than as an optical cladding.
Subsequent to formation of this firs-t barrier layer or ~ ~
absent such procedure, where the tube is of sufficlent ~-purity, reactant materials of such nature as to result in the desired index-increased core are introduced. In a chloride system, these may take the form of a mixture of SiC14 together with, for example GeC14, and oxygen.
Chlorides of other index increasing materials, such as ~`~
phosphorus, titanium and aluminum may be substituted for GeC14 or admixed. BC13 may also be included perhaps to facilitate glass formation because of lowered fusion temperature; or because of refractiva index l~wering, the initial mixture may be altered during successi~e hot zone traversals so as to increase index (by increasing GeC14 or ~
other index-lncreasing dopant precursor or by decreasing ~ ;
BC13) Since the usual vapor phase glass precursor compounds are not oxidic, oxygen or a suitable oxygen bearing compound is generally included to form the ultimate oxidic glass. A satisfactory procedure, followed in exemplary procedures, takes the form of an oxygen stream bubbled through reservoirs of li~uid phase glass forming compounds. In one procedure, for example, oxygen streams were bubbled through silicon tetrachloride, and through germanium tetrachloride. These streams were then combined with vapor phase boron trichloride and additional oxygen, the resultant mixture being introduced into the reaction chamber.
Relative amounts of glass forming ingred~ents are .
~, .. . . . . . . .
MacChesney-olconnor 9_1l ~V~JI~ , 1 dependent upon a variety o~ factors, such as vapor 2 pressure, temperature, flow rate, desired index, etc.
3 The appended examples indicate suitable amounts f'or producing L~ the noted indices under -the noted conditions. Variants are known to those f`amiliar wi-th glass forming procedures.
6 A variety of diluent ma-terials may be utilized for ;~
7 any of' the noted reasons so, for example, argcn, nitrogen, 8 helium, etc., may serve to maintain desired f'low rates to ;
9 prevent precombustion, etc. Oxygen bearing compounds which ; ;-may replace oxygen in whole or in part include N20, NO, and 2' 12 In general, concentration of 3d-transition metal 13 impurities in the gas stream is kept below 10 percent, 14 although furtAer reduction in loss accompanies reduction of' those impurities down to the part per billion range. Such 16 levels are readiIy available from commercial sources or by 17 purification by means similar to those taught by H.C.
18 Theuerer, U.S. Patent No. 3~07],444. As compared with the 19 usual soot process, the inventive procedure is carried out in a controlled environment without direct exposure to 21 combustion products. This inherently results in avoidance 22 of inclusion of particula-te combustion products. Where 23 desired, h~dra-tion resulting from combustion in the soot 24 process may be minimized. This is a particularly significant advantage for operation in several portions of the infrared 26 spectrum which suffers from sub-harmonics of' the f`undamental 27 H O absorption. Water vapor may, therefore, be a 28 particularly significant impurity and, for many purposes, 29 should be kept to a level below a few ppm by ~olume.
3. General Procedure 31 The procedure described is that which was followed ~ : .
.~
~ ',.
~ .. . . . . . .. . . .
~l)S~ 3 in Examples 1 through 4O Deposition was carried out within a 12 I.D. by 14 O.D. mm silica tube. The tube was placed on a glass lathe within which it was rotated a-t 100 rpm~
Before in-troduction of reactants, it was flushed with a continuous stream of oxygen while -traversing with an oxyhydrogen burner sufficient to bring the wall temperature to 1400 degrees C. The purpose was to remove any volatile impurities on the inside wall of the tube.
Following a period of 5 minutes, a mixture of lC oxygen, SiC14, and BC13 replaced the oxygen flow. The composition of approxima'cely 10 percent ~iC14, 3 percent BC13, remainder oxygen, maintaining temperature at 1400 degrees C within the moving hok zone as measured at the wall. In this particular example, the zone was moved at a speed of approximately 45 cm/min in the forward direction (direction of gas flow) and was rapidly returned to its ~`
initial position (approximately 30 sec. elapsed time to the beginning of the slow traversal).
Formation of flaky material within the tube, at a position spaced from the wall generally downstream of the hot zone, was visually observed. It was deduced and verified that homogeneous reaction was largely within the zone with particulates being carried downstream by the moving gas. Deposition was continued for approximately twenty minutes following which flow of chloride reactants was discontinued. Oxygen flow was continued for several passes of the hot zone.
The procedure to this point results in deposition of a layer serving as cladding. Core material was next deposited by introduction of SiC14 and GeC14. These reactants, too, were introduced with an oxygen carrier, as ., ' .. ~ ,, . ~ , . . . . . .
~S0~33 ~:
before. With the temperature of the hot zone increased somewhat to about 1450 degrees C, deposition was continued -for about one hour.
In this particular example, tube collapse was in:itiated with reactants still flowing simply by reducing the rate of traverse of the hot zone. This resulted in a ; temperature increase which ultimately attained a level of about 1900 degrees C to produce nearly complete collapse.
Reactant flow was then stopped with final collapse producing a finished preform consisting of a GeO2-SiO2 core with a borosilicate cladding supported, in turn, by a silica layer.
It will be recognized by those skilled in the art of fiber drawing, that the tube, without first being collapsed, can also be drawn into acceptable fiber. ~he resulting preform was then drawn to result in a fiber having an overall diameter of approximately 100 ~m with a core area defined . . , , ~ ~
as the region within the borosilicate layer having a ~ -diameter of approximately 37 ~m. The length of fiber drawn ~
:
was approximately 0.7 km. The method described in some detail in N.S. Kapany, Fiber Optics Principles a d Applications (Academic Press, New York) (1967) pages 110-117, involved ~ ~-;. ~. ~;;.
the local heating of an end of the preform which was affixed to the fiber, which was, in turn, drawn at a constant velocity of approximately 60 meters/min by winding on a 30 cm diameter ;
mandrel rotating at 60 rpm.
~; The above description is in exemplary terms and is usefully read in conjunction with the appended examples.
,.~; .
The inventive process departs from conventional CVD as described--i.e., in that reactant introduction rate and -;~
temperature are such as to result in homogeneous reaction to -;~
produce oxidic particles within the space enclosed, but :' '. ' ', ; 14 ., .: , .
~acChesney-O'Connor 9-4 1 separated from the walls of a tube. Thls, when combined 2 wlth a moving hot zone~ results ln rapld preparation of a 3 hlgh quality preform as descrlbed. The movlng hot zone i5 4 responsible for (1) homogeneous reactlon; (2) to a large extent, the adherence of oxldlc particles -to the wall; and 6 (3) fuslon of the deposlted particles and CVD-produced layer 7 into a unitary, homogeneous glassy layer. In general, it is 8 deslrable to maintaln the hot zone as short as posslble 9 depending upon constancy of traversal speed to result in uniform layer-production. Motlon of the hot zone should be 11 such -that every portion of -the tube ls heated to the zone 12 temperature for the same perlod of time. I'hls is easily 13 accompllshed by passlng the heating means through a 14 traversal dlstance whlch extends beyond the tube at both ends. Experimentally, hot zones of the order of 2 cm length 16 (defining the heated region extending 4 cm on either side of 17 the peak) have resulted in uniform coating under all 18 experimental condltlons. Whlle, ln prlnciple, heating the 19 entlre tube may result ln uniformity of depositlon approachlng that attained by use of a moving zone, very high 21 flow rates are required to avoid inhomogeneity and 22 differing thickness of deposit along the length of the tube.
23 4. Examples ~ 24 The following examples, utlllzing chlorlde or i 25 hydrlde reactants, are set forth. The selection was made 26 wlth a vlew to demonstrating a wlde varlety of composltlons 27 and dlfferent types of optical wavegulde preforms for whlch 28 the procedure can be used.
29 The tube of commerclal grade fused quartz was 3 flrst cleaned by lmmerslon ln hydrofluoric acid-~nitric acid 31 solution for three minutes and was rinsed with delonlzed water for a period of one hour. Tubing was cut into 18"
lengths, and such sections were utilized in each of the examples. The substrate tube was provided with appropriate input and exhaust sections, and was heated with a moving oxyhydrogen torch producing a hot zone which traversed the tube in from one to eight minutes. In each instance, flushing was by oxygen at a flow rate of between 100 and 500 cm3/min corresponding with a linear rate of 4.5 meter/mins, and this flushing was continued for several traversals of the zone.
Example 1 The fused quartz tube used in this example was 12 mm I.D. x 14 mm O.D. Initial deposition was of a cladding material, Sio2-B203, by introduction of 41 cm3/min.
SiC14, 12.5 cm3/min BC13, both carried by oxygen such that the total oxygen flow was 250 cc/min. Sixteen passes of the ~;
., ~ . .
hot zone were made at a temperature of 1430 degrees C. Core material was next deposited by flows of 32 cc/min SiC14, 48 cc/min GeC14, and oxygen 650 cc/min. This was continued for 68 minutes and temperatures of the hot zone were maintained at 1460 degrees C. Remaining steps, including partial collapse with flowing gas and final collapse under ~
no flow conditions, were as specified under Section 3. The ;~;
fiber that resulted from this procedure had a core of approximately 40 ~m with an overall diameter of approximately 100 ~m. Its length was 723 meters and optical attenuation was 2 dB/km at 1060-1100 nm.
Example 2 ;~
A fused quartz tube 6 mm I.D. x 8 mm O.D. was 30 cleaned as described and positioned in a glass lathe. Flows of diluted (1 percent by volume in N2) silane, germane, ~ -16-, - 1C~5~)833 diborane, and oxyyen were passed through the tube as follows:
SiH4 1,000 cc/min.
Ge~4 150 cc/min.
B2~l6 50 cc/min.
Deposition commenced by heating the tube locally using an oxyhydrogen flame which was traversed along the length of the tube. The complete cycle took 3.7 minutes, and the highest temperature attained was 1400 degrees C. After 175 minutes, the gas flows were stopped and the tube collapsed in one additional pass, made at a much slower ~ -~
rate. Temperatures achieved here were in the vicinity oE
1750-1900 degrees C. The preform was removed to a pulling apparatus and drawn to a fiber whose diameter was 100 microns overall. This consisted of a core whose composition was SiO2-GeO2-B2O3 of approximately 25 microns diameter. The cladding had the composition of SiO . The index difference produced by the core was 0.007.
Example 3 A clean fused silica tube 6 mm I.D. x 8 mm O.D.
was positioned in a glass lathe as previously described.
Flows of diluted (3.05 percent by volumn in M2) silane, diborane, and oxygen were passed through the tube as follows: -SiH4 295 cc/min. ~-;
.' :
B2H6 49 cc/min.
2 900 cc/min.
~; Deposition commenced by heating the tube locally using an oxyhydrogen torch which traversed along the tube at a rate of 0.10 cm/sec as the tube rotated at 100-120 rpm.
The torch was adjusted so as to produce a temperature ~ .:
: ~17- ~
, ` ' --- MacChesney-O'connor 9-4 ~Lal5~8~3 1 locally o~ 1375-1450 degrees ~. When the torch had moved 2 to the end of the -tube, it ~as returned at 0.15 cm/sec with 3 the SiHl~ and B2H6 flows stopped~ This procedure continued for 4 three hours. At this time the B H6 flow was s-topped and ~ust SiH4 and 2 continued. At the same time, the torch was 6 ad~usted to produce temperatures of 1600-1650 degrees C3 ?
7 other conditions remaining the same as previously.
8 Depositing the pure sio2 layer continued for 1.5 hours.
g ~t this time, silane flow was stopped and just 0 flow continued at 600 cc/min. Temperatures were varied 11 during the next two passes to 1650-1700 degrees C. Now the 12 oxygen was stopped, the traverse slowed to 0.05 cm/sec, and 13 the temperature raised to 1850-1890 degrees C to bring about 14 complete collapse of the tube.
This procedure produced a preform having a core of 16 pure SiO2, a cladding layer of B203-SiO2~ and an outer 17 jacket of commercial grade SiO . The fiber drawn from this 18 preform had a core o~ 30 ~ m, cladding thickness of 15~ m 19 and an outer jacket of 20~ m, with an index difference of 0.007 percent and losses of 3 dB/km at 1.06~m wavelength.
21 Example 4 22 For optical communications employing multimode 23 optical fibers it is desirable to more nearly equalize the 24 group velocities of propagating modes. This result is 25 expscted if the index of the core is gradually increased ; ~.
26 from the cladding toward the interior of the core. To 27 accomplish this a 8 mm I.D. x 10 mm 0 D. fused quartz tube 28 was positioned and borosilicate layer intended to serve as 29 a portion of the cladding and as a barrier layer was 30 deposited as in Example 1. Next deposition of the GeO2 -; 31 B203 - SiO2 core was commenced except that the germania 32 content was _ 18 -~ '.
1C~5;~833 gradually increased from zero during the period of deposition. The conditions used duriny the deposition were as follows:
Barrier layer SiC14 32 cc/min BC13 12.5 cc/min 2 250 cc/min Temp 1740 degrees C
Time 25 min;
Graded Index portion of the core SiC14 33 cc/min BC13 12.5 7.5 cc/min 17 equal increments at 2 min intervals GeCl~ 0 - 35 cc/min 17 equal increments at 2 min intervals -; 2 460-830 cc/min 17 equal increments at 2 min intervals ~-Temp 1470 degrees C ~
Constant Index portion of core ~-SiC14 32 cc/min BC13 7-5 cc/min GeC14 35 cc/mln ~; 2 830 cc/min Temp 1470 degrees C
Time 53 min. ;
At the conclusion of the deposition, the tube was collapsed to yield a solid preform which was then pulled to .
~ yield an optical fiber. When the mode dispersion of this . . .
fiber was measured, it behaved in a manner expected oE a 3Q graded index. This behavior can be expressed by relation ;~ (Bell System Technical Journal 52, pp. 1566 (1973)) = nO[l-2~(r/a)~]l/2 where in this instance the value of ~ = 5.
: - 1 9 . ' :' ~
~ .. .. . . . . . .
12 Brief Description of the Drawing 13 FIG. 1 is a front elevational view of apparatus 14 suitable for practice of the deposi-tion process in accordance with the invention;
16 FIG. 2 is a front elevational view of apparatus ;
17 alternative to that of FIG. l;
18 FIG. 3 is a front elevational view of a section of 19 tubular material depic-ting observed conditions during processing; and 21 FIG. 4, on coordinates of insertion loss in units 22 of dB/kilometer and wavelength in nanome-ters, is a plot 23 showing the relationship of those two parameters for a clad 24 multimode fiber produced in accordance wi-th the invention.
Detailed Description -~
26 1. The Drawing . .
27 FIG. 1 depicts a lathe 1 holding substrate tube 2 28 within which a hot zone is produced by heating means 3 and 29 4 Tube 2 may be rotated, for example, in the direction shown by arrow 5a by means not shown and hot zone is caused 31 to traverse tube 2 by movement of heating means 3 and 32 support 4 as - 6 _ - MacChesney-O'Connor 9-~
1 schematically depicted by double headed arrow 5b, for 2 example, by a threaded feed member 6. ~ gaseous material is 3 introduced into tube 2 via inlet tube 7 which is, in turn, 4 connected to source material reservoirs 8. Such reservoirs may include an oxygen inlet 9 connected to means not shown.
6 As depicted, gaseous material ma~ also be introduced by inlets 7 10 and 11 by means not shown and through in]et 12 from 8 reservoir 13. Reservoirs 14 and 15 contain normally li~uid 9 reactant material which is introduced into tube 2 by means of carrier gas introduced through inlets 10 and 11 with the be;~a 11 arrangement ~ ~ch that the carrier gas is bubbled through 12 such liquids 16 and 17. Exiting material is exhausted -through 13 outlet 18. Not shown is the arrangement of mixing valves 14 and shut off valves which may be utilized to meter ~lows and to make other necessary adjustments in composition. The 16 apparatus of FIG. 1 is generally horizontally disposed. ~ `~
17 The apparatus of FIG. 2 is, in its operational 18 characteristic, quite similar to that o~ FIG. 1. Vertical 19 disposition of the substrate tube, however, lends stability ., .
to the portion of the tube within the hot zone and may 21 permit attainment of higher temperature or o~ longer hot 22 zones in the traversal direction without objectionable 23 dis-tortion. Apparatus depicted includes tube 20 which may .
24 optionally be provided with rotation means not shown. This tube ~s secured to the apparatus by means o~ chucks 21 and 26 22 and a traversing hot zone is produced within tube 20 27 by means of a ring burner 23 which is caused to constantly 28 traverse tube 20 in the direction depicted by double headed 29 arrow 24 by moving means 25. Gaseous material, for example, ~rom source such as 8 o~ FIG. 1 is introduced via inlet 7 ~ -~50833 tube 26 and e~iting material leaves via exhaust 27.
FIG. 3 is a front elevational view o~ a section of a substrate tube 30 as observed during deposition. Depicted is a heating means 31 producing a hot zone 32 which is traversing tube 30 in the direc-tion shown by arrow 33 by means not shown. Gaseous material is introduced at the :Left end of tube 30 and flows in the broken section of the Figure in the direction shown by arrow 34. For the processing conditions, which with respect to traversal direction and hot zone temperature are those of Example l, two regions are clearly observable. Zone 35 downstream of hot zone 32 is filled with a moving powdery suspension of particulate oxidic material, while region 36, devoid of such particulate matter, defines the region within which fusion of deposited material is occurring.
FIG. 4 is a plot for measured loss in uni~s of dB/kilometer as measured on 713 meters of fiber prepared in accordance with an Example herein. Abscissa units are wavelength in nanometers. It is seen that loss is at a minimum of about 2 dB/kilometer for the wavelength range of about 1060 to 1100 nm (the limiting value on the plot). The peak at about 950 nm, as well as those at 880 and 730 nm, are characteristic sub-harmonics of the fundamental water absorption.
2. Processing Re~uirements -a. Reaction Temperature Superficially, the inventive technique resembles conventional chemical vapor deposition. However, whereas CVD conditions are so arranged that deposition is solely the result of heterogeneous formation at a heated substrate surface, procedures of this invention rely upon significaht .
, ``~ ` 1(3154C~833 homogeneous reaction. In generalj 50 percent or more of reaction product is produced in a position removed from substrate surface and results in the formation of solid~
oxidic particles of the desired glass composition. These particles are similar to -those produced during the "soot"
process.
Homogeneous reaction is the result of sufficient rate of reactant introduction and sufficient reaction temperature. Such conditlons may be achieved simply by increasing one or both parameters until homogeneous reaction i9 visually observed. To optimize the process from the ~ ;~
standpoint of reaction, high temperatures are utilized. For `~
the usual silica based systems which comprise the preferred embodiment, temperatures at least at the substrate wall are ; generally maintained at a minimum oE 1200 degrees C at the moving position corresponding with the hot 20ne. Maximum a ` : :~
tempe ~ ures are ultimately limited by significant wall distortion. For horizontally disposed apparatus, ~uch as ~ that shown in FIG. 1, in which a hot zone of the length of ~ 20 approximately 2 cm moves at the!rate of about 45 cm/min within a tube rotated at the rate of about 100 rpm~ a temperature of 1600 degrees C may be produced without ~;
harmful tube distortion. Decreasing the length of the hot , . ~
zone, increasing the rate of rotation, increasing reactant flow rate, vertical disposition of the tube, are all factors .,:: .
which may permit use of higher maximum temperatures without ;~
variation in tube geometry. Indicated temperatures are those measured by means of an optical pyrometer focused at the outer tube surface. It has been estimated that for :
typical conditions the thermal gradient across the tube may be as high as 300 degrees C.
:
~ _ g _ ' : :' :~
.
: ,, . . . ~ , .
b. Flow Rates This parameter, like temperature, is dependen-t upon other processing conditions. Again, a ~inimum accep-table rate for those purposes may be determined by visual observation.
~ighest flow rates are ~or those materials which by virtue of combustibility, high vapor pressure, etc., are diluted to a signiEicant extent by inert material. Examples are the hydrides where dilution frequently is as high as 99.5 volume percent based on the total reactant content may necessitate a linear flow rate of at least 1 m~ter per second. Chlorides, ;
which do not present this problem, need not be diluted to avoid combustion. Inert material, such as nitrogen or helium, is introduced solely for transfer purposes and need b~ present only in amount typically of up to 10 percent by volume.
Flow rates are, as indicated, temperature dependent, with the required homogeneous reaction taking place at acceptable rate only by an increase flow of about 50 percent for each hundred degree increase in reaction temperature.
c. Reactants Examples were carried out using chlorides and hydrides. Other gaseous materials of sufficient vapor pressure under processing conditions preferably which react with oxygen or oxygen bearing material to produce the required oxidic glass may be subs'cituted. In a typical system, the substrate tube is silica-~generally undoped. Where this -~ tube is of ordinary purity, first reactant introduced may be such as to result in the formation of a flrst layer of undoped silica or doped with an oxide such as B2O3 which serves to lower the refractive index, which acts as a part of the clad and presents a barrier to diffusing impurlty -10- . ~
~50~333 from the tube. It may be considered that, under these - circumstances, the substrate tube ultimately serves as a mechanical support rather than as an optical cladding.
Subsequent to formation of this firs-t barrier layer or ~ ~
absent such procedure, where the tube is of sufficlent ~-purity, reactant materials of such nature as to result in the desired index-increased core are introduced. In a chloride system, these may take the form of a mixture of SiC14 together with, for example GeC14, and oxygen.
Chlorides of other index increasing materials, such as ~`~
phosphorus, titanium and aluminum may be substituted for GeC14 or admixed. BC13 may also be included perhaps to facilitate glass formation because of lowered fusion temperature; or because of refractiva index l~wering, the initial mixture may be altered during successi~e hot zone traversals so as to increase index (by increasing GeC14 or ~
other index-lncreasing dopant precursor or by decreasing ~ ;
BC13) Since the usual vapor phase glass precursor compounds are not oxidic, oxygen or a suitable oxygen bearing compound is generally included to form the ultimate oxidic glass. A satisfactory procedure, followed in exemplary procedures, takes the form of an oxygen stream bubbled through reservoirs of li~uid phase glass forming compounds. In one procedure, for example, oxygen streams were bubbled through silicon tetrachloride, and through germanium tetrachloride. These streams were then combined with vapor phase boron trichloride and additional oxygen, the resultant mixture being introduced into the reaction chamber.
Relative amounts of glass forming ingred~ents are .
~, .. . . . . . . .
MacChesney-olconnor 9_1l ~V~JI~ , 1 dependent upon a variety o~ factors, such as vapor 2 pressure, temperature, flow rate, desired index, etc.
3 The appended examples indicate suitable amounts f'or producing L~ the noted indices under -the noted conditions. Variants are known to those f`amiliar wi-th glass forming procedures.
6 A variety of diluent ma-terials may be utilized for ;~
7 any of' the noted reasons so, for example, argcn, nitrogen, 8 helium, etc., may serve to maintain desired f'low rates to ;
9 prevent precombustion, etc. Oxygen bearing compounds which ; ;-may replace oxygen in whole or in part include N20, NO, and 2' 12 In general, concentration of 3d-transition metal 13 impurities in the gas stream is kept below 10 percent, 14 although furtAer reduction in loss accompanies reduction of' those impurities down to the part per billion range. Such 16 levels are readiIy available from commercial sources or by 17 purification by means similar to those taught by H.C.
18 Theuerer, U.S. Patent No. 3~07],444. As compared with the 19 usual soot process, the inventive procedure is carried out in a controlled environment without direct exposure to 21 combustion products. This inherently results in avoidance 22 of inclusion of particula-te combustion products. Where 23 desired, h~dra-tion resulting from combustion in the soot 24 process may be minimized. This is a particularly significant advantage for operation in several portions of the infrared 26 spectrum which suffers from sub-harmonics of' the f`undamental 27 H O absorption. Water vapor may, therefore, be a 28 particularly significant impurity and, for many purposes, 29 should be kept to a level below a few ppm by ~olume.
3. General Procedure 31 The procedure described is that which was followed ~ : .
.~
~ ',.
~ .. . . . . . .. . . .
~l)S~ 3 in Examples 1 through 4O Deposition was carried out within a 12 I.D. by 14 O.D. mm silica tube. The tube was placed on a glass lathe within which it was rotated a-t 100 rpm~
Before in-troduction of reactants, it was flushed with a continuous stream of oxygen while -traversing with an oxyhydrogen burner sufficient to bring the wall temperature to 1400 degrees C. The purpose was to remove any volatile impurities on the inside wall of the tube.
Following a period of 5 minutes, a mixture of lC oxygen, SiC14, and BC13 replaced the oxygen flow. The composition of approxima'cely 10 percent ~iC14, 3 percent BC13, remainder oxygen, maintaining temperature at 1400 degrees C within the moving hok zone as measured at the wall. In this particular example, the zone was moved at a speed of approximately 45 cm/min in the forward direction (direction of gas flow) and was rapidly returned to its ~`
initial position (approximately 30 sec. elapsed time to the beginning of the slow traversal).
Formation of flaky material within the tube, at a position spaced from the wall generally downstream of the hot zone, was visually observed. It was deduced and verified that homogeneous reaction was largely within the zone with particulates being carried downstream by the moving gas. Deposition was continued for approximately twenty minutes following which flow of chloride reactants was discontinued. Oxygen flow was continued for several passes of the hot zone.
The procedure to this point results in deposition of a layer serving as cladding. Core material was next deposited by introduction of SiC14 and GeC14. These reactants, too, were introduced with an oxygen carrier, as ., ' .. ~ ,, . ~ , . . . . . .
~S0~33 ~:
before. With the temperature of the hot zone increased somewhat to about 1450 degrees C, deposition was continued -for about one hour.
In this particular example, tube collapse was in:itiated with reactants still flowing simply by reducing the rate of traverse of the hot zone. This resulted in a ; temperature increase which ultimately attained a level of about 1900 degrees C to produce nearly complete collapse.
Reactant flow was then stopped with final collapse producing a finished preform consisting of a GeO2-SiO2 core with a borosilicate cladding supported, in turn, by a silica layer.
It will be recognized by those skilled in the art of fiber drawing, that the tube, without first being collapsed, can also be drawn into acceptable fiber. ~he resulting preform was then drawn to result in a fiber having an overall diameter of approximately 100 ~m with a core area defined . . , , ~ ~
as the region within the borosilicate layer having a ~ -diameter of approximately 37 ~m. The length of fiber drawn ~
:
was approximately 0.7 km. The method described in some detail in N.S. Kapany, Fiber Optics Principles a d Applications (Academic Press, New York) (1967) pages 110-117, involved ~ ~-;. ~. ~;;.
the local heating of an end of the preform which was affixed to the fiber, which was, in turn, drawn at a constant velocity of approximately 60 meters/min by winding on a 30 cm diameter ;
mandrel rotating at 60 rpm.
~; The above description is in exemplary terms and is usefully read in conjunction with the appended examples.
,.~; .
The inventive process departs from conventional CVD as described--i.e., in that reactant introduction rate and -;~
temperature are such as to result in homogeneous reaction to -;~
produce oxidic particles within the space enclosed, but :' '. ' ', ; 14 ., .: , .
~acChesney-O'Connor 9-4 1 separated from the walls of a tube. Thls, when combined 2 wlth a moving hot zone~ results ln rapld preparation of a 3 hlgh quality preform as descrlbed. The movlng hot zone i5 4 responsible for (1) homogeneous reactlon; (2) to a large extent, the adherence of oxldlc particles -to the wall; and 6 (3) fuslon of the deposlted particles and CVD-produced layer 7 into a unitary, homogeneous glassy layer. In general, it is 8 deslrable to maintaln the hot zone as short as posslble 9 depending upon constancy of traversal speed to result in uniform layer-production. Motlon of the hot zone should be 11 such -that every portion of -the tube ls heated to the zone 12 temperature for the same perlod of time. I'hls is easily 13 accompllshed by passlng the heating means through a 14 traversal dlstance whlch extends beyond the tube at both ends. Experimentally, hot zones of the order of 2 cm length 16 (defining the heated region extending 4 cm on either side of 17 the peak) have resulted in uniform coating under all 18 experimental condltlons. Whlle, ln prlnciple, heating the 19 entlre tube may result ln uniformity of depositlon approachlng that attained by use of a moving zone, very high 21 flow rates are required to avoid inhomogeneity and 22 differing thickness of deposit along the length of the tube.
23 4. Examples ~ 24 The following examples, utlllzing chlorlde or i 25 hydrlde reactants, are set forth. The selection was made 26 wlth a vlew to demonstrating a wlde varlety of composltlons 27 and dlfferent types of optical wavegulde preforms for whlch 28 the procedure can be used.
29 The tube of commerclal grade fused quartz was 3 flrst cleaned by lmmerslon ln hydrofluoric acid-~nitric acid 31 solution for three minutes and was rinsed with delonlzed water for a period of one hour. Tubing was cut into 18"
lengths, and such sections were utilized in each of the examples. The substrate tube was provided with appropriate input and exhaust sections, and was heated with a moving oxyhydrogen torch producing a hot zone which traversed the tube in from one to eight minutes. In each instance, flushing was by oxygen at a flow rate of between 100 and 500 cm3/min corresponding with a linear rate of 4.5 meter/mins, and this flushing was continued for several traversals of the zone.
Example 1 The fused quartz tube used in this example was 12 mm I.D. x 14 mm O.D. Initial deposition was of a cladding material, Sio2-B203, by introduction of 41 cm3/min.
SiC14, 12.5 cm3/min BC13, both carried by oxygen such that the total oxygen flow was 250 cc/min. Sixteen passes of the ~;
., ~ . .
hot zone were made at a temperature of 1430 degrees C. Core material was next deposited by flows of 32 cc/min SiC14, 48 cc/min GeC14, and oxygen 650 cc/min. This was continued for 68 minutes and temperatures of the hot zone were maintained at 1460 degrees C. Remaining steps, including partial collapse with flowing gas and final collapse under ~
no flow conditions, were as specified under Section 3. The ;~;
fiber that resulted from this procedure had a core of approximately 40 ~m with an overall diameter of approximately 100 ~m. Its length was 723 meters and optical attenuation was 2 dB/km at 1060-1100 nm.
Example 2 ;~
A fused quartz tube 6 mm I.D. x 8 mm O.D. was 30 cleaned as described and positioned in a glass lathe. Flows of diluted (1 percent by volume in N2) silane, germane, ~ -16-, - 1C~5~)833 diborane, and oxyyen were passed through the tube as follows:
SiH4 1,000 cc/min.
Ge~4 150 cc/min.
B2~l6 50 cc/min.
Deposition commenced by heating the tube locally using an oxyhydrogen flame which was traversed along the length of the tube. The complete cycle took 3.7 minutes, and the highest temperature attained was 1400 degrees C. After 175 minutes, the gas flows were stopped and the tube collapsed in one additional pass, made at a much slower ~ -~
rate. Temperatures achieved here were in the vicinity oE
1750-1900 degrees C. The preform was removed to a pulling apparatus and drawn to a fiber whose diameter was 100 microns overall. This consisted of a core whose composition was SiO2-GeO2-B2O3 of approximately 25 microns diameter. The cladding had the composition of SiO . The index difference produced by the core was 0.007.
Example 3 A clean fused silica tube 6 mm I.D. x 8 mm O.D.
was positioned in a glass lathe as previously described.
Flows of diluted (3.05 percent by volumn in M2) silane, diborane, and oxygen were passed through the tube as follows: -SiH4 295 cc/min. ~-;
.' :
B2H6 49 cc/min.
2 900 cc/min.
~; Deposition commenced by heating the tube locally using an oxyhydrogen torch which traversed along the tube at a rate of 0.10 cm/sec as the tube rotated at 100-120 rpm.
The torch was adjusted so as to produce a temperature ~ .:
: ~17- ~
, ` ' --- MacChesney-O'connor 9-4 ~Lal5~8~3 1 locally o~ 1375-1450 degrees ~. When the torch had moved 2 to the end of the -tube, it ~as returned at 0.15 cm/sec with 3 the SiHl~ and B2H6 flows stopped~ This procedure continued for 4 three hours. At this time the B H6 flow was s-topped and ~ust SiH4 and 2 continued. At the same time, the torch was 6 ad~usted to produce temperatures of 1600-1650 degrees C3 ?
7 other conditions remaining the same as previously.
8 Depositing the pure sio2 layer continued for 1.5 hours.
g ~t this time, silane flow was stopped and just 0 flow continued at 600 cc/min. Temperatures were varied 11 during the next two passes to 1650-1700 degrees C. Now the 12 oxygen was stopped, the traverse slowed to 0.05 cm/sec, and 13 the temperature raised to 1850-1890 degrees C to bring about 14 complete collapse of the tube.
This procedure produced a preform having a core of 16 pure SiO2, a cladding layer of B203-SiO2~ and an outer 17 jacket of commercial grade SiO . The fiber drawn from this 18 preform had a core o~ 30 ~ m, cladding thickness of 15~ m 19 and an outer jacket of 20~ m, with an index difference of 0.007 percent and losses of 3 dB/km at 1.06~m wavelength.
21 Example 4 22 For optical communications employing multimode 23 optical fibers it is desirable to more nearly equalize the 24 group velocities of propagating modes. This result is 25 expscted if the index of the core is gradually increased ; ~.
26 from the cladding toward the interior of the core. To 27 accomplish this a 8 mm I.D. x 10 mm 0 D. fused quartz tube 28 was positioned and borosilicate layer intended to serve as 29 a portion of the cladding and as a barrier layer was 30 deposited as in Example 1. Next deposition of the GeO2 -; 31 B203 - SiO2 core was commenced except that the germania 32 content was _ 18 -~ '.
1C~5;~833 gradually increased from zero during the period of deposition. The conditions used duriny the deposition were as follows:
Barrier layer SiC14 32 cc/min BC13 12.5 cc/min 2 250 cc/min Temp 1740 degrees C
Time 25 min;
Graded Index portion of the core SiC14 33 cc/min BC13 12.5 7.5 cc/min 17 equal increments at 2 min intervals GeCl~ 0 - 35 cc/min 17 equal increments at 2 min intervals -; 2 460-830 cc/min 17 equal increments at 2 min intervals ~-Temp 1470 degrees C ~
Constant Index portion of core ~-SiC14 32 cc/min BC13 7-5 cc/min GeC14 35 cc/mln ~; 2 830 cc/min Temp 1470 degrees C
Time 53 min. ;
At the conclusion of the deposition, the tube was collapsed to yield a solid preform which was then pulled to .
~ yield an optical fiber. When the mode dispersion of this . . .
fiber was measured, it behaved in a manner expected oE a 3Q graded index. This behavior can be expressed by relation ;~ (Bell System Technical Journal 52, pp. 1566 (1973)) = nO[l-2~(r/a)~]l/2 where in this instance the value of ~ = 5.
: - 1 9 . ' :' ~
~ .. .. . . . . . .
Claims (25)
PROPERTY OR PRIVILEGE IS CLAIMED AXE DEFINED AS FOLLOWS:
1. Process for fabrication of a glass fiber optical trans-mission line, comprising a core section and a cladding, wherein the cladding has an index of refraction of a value lower than the maximum index of the core for energy of the wavelength to be transmitted, comprising introducing a moving stream of a vapor mixture including at least one compound glass-forming precursor together with an oxidizing medium into a tube while heating the tube so as to react the said mixture and produce a glassy deposit on the inner surface of the tube, characterized in that heating of tube and contents are by a moving hot zone produced by a correspondingly moving heat source external to the tube in that combustion within the tube is avoided and in that temperature within the hot zone, composition of the vapor mixture, and rate of introduction of the vapor mixture are maintained at values such that at least a part of the reaction takes place within the gaseous mixture at a position spaced from the inner walls of the said tube, thereby producing a suspension of oxidic reaction product particulate material, whereby the particulate material while traveling downstream comes to rest on the inner surface of the tube within a region which extends from a position within the said hot zone, the moving zone serving the dual functions of: nucleation site for homo-geneous reaction to produce particulate matter; and consolidation site for previously produced particulate matter.
2. Process of claim 1 in which the vapor mixture includes a silicon-bearing compound as a glass compound precursor.
3. Process of claim 2 in which an oxidizing medium is oxygen.
4. Process of claim 3 in which the maximum temperature within the hot zone during traversal is at least 1200 degrees C.
5. Process of claim 1 in which the tube is rotated during processing.
6. Process of claim 1 in which the tube is disposed essentially horizontally during processing and in which the tube is rotated axially at a rate of at least 10 rpm.
7. Process of claim 1 in which the tube is disposed essentially vertically.
8. Process of claim 1 in which the composition of glass precursor is varied at least once during processing.
9. Process of claim 8 in which the variation in composition of the glass percursor is such as to result in index of refraction which increases with successive depositions.
10. Process of claim 9 in which the composition of the initial glass deposit is primarily silica.
11. Process of claim 10 in which the initial deposit includes boron oxide.
12. Process of claim 9 in which the composition of the glassy deposit is varied so as to result in at least a region of increasing refractive index in a radial direction toward the center.
13. Process of claim 1 in which the said mixture includes chlorides of the cations to be included in the glassy deposit.
14. Process of claim 1 in which the said mixture includes hydrides of the cations to be included in the glassy deposit and in which the said mixture includes an inert gaseous diluent.
15. Process of claim 1 in which the hot zone temperature is increased after initial processing so as to result in at least partial collapse of the said tube.
16. Process of claim 15 in which the increase in temperature is produced by decreasing the rate of traversal of the said hot zone.
17. Process of claim 15 in which the temperature is ultimately increased to a level sufficient to result in complete collapse of the tube and deposit, thereby producing a solid preform structure.
18. Process of claim 17 in which the said preform structure is drawn to produce a fiber.
19. Process of claim 18 in which drawing is sufficient to produce an ultimate outer diameter of the order of 100 µm.
20. Process of claim 19 in which the tube is retained as a portion of the said preform so that a reduced version of the core is retained in the final fiber.
21. Process of claim 19 in which the fiber cross-section portion corresponding with glassy material deposited during the said method has a diameter of at least 30 µm.
22. Process of claim 1 in which the said tube and glassy deposit is drawn to produce the said line.
23. Process of claim 22 in which the said tube and deposit is at least partially collapsed prior to drawing.
24. A process of fabricating a preform for drawing into a glass fiber optical transmission line comprising introducing into a rotating glass tube, the inner surface of which is made up of a glass having a first refractive index, a gaseous mixture of oxygen and chlorides of silicon and germanium while a hot zone moving repeatedly along said tube is produced inside said tube by a heat source external to said tube, while maintaining the temperature of the hot zone sufficiently high and introducing said silicon and germanium chlorides at a sufficient rate that the silicon and germaniuim are converted to an oxidic product at least partly in the form of entrained particulate material which comes to rest on the inner surface of the tube, the temperature being sufficiently high to effect fusion of said deposited particulate material into a unitary glassy layer of a refractive index higher than said first refractive index.
25. Process of claim 24 in which the said vapor mixture includes a hydride and also includes diluent to avoid combustion.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US44470574A | 1974-02-22 | 1974-02-22 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1050833A true CA1050833A (en) | 1979-03-20 |
Family
ID=23766003
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA219,629A Expired CA1050833A (en) | 1974-02-22 | 1975-02-07 | Optical fiber fabrication involving homogeneous reaction within a moving hot zone |
Country Status (6)
| Country | Link |
|---|---|
| JP (1) | JPS5522423B2 (en) |
| CA (1) | CA1050833A (en) |
| DE (1) | DE2507340B2 (en) |
| FR (1) | FR2261992B1 (en) |
| GB (1) | GB1500530A (en) |
| NL (1) | NL165720C (en) |
Families Citing this family (34)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4360250A (en) * | 1974-05-31 | 1982-11-23 | National Research Development Corp. | Optical waveguides |
| JPS5156642A (en) * | 1974-11-13 | 1976-05-18 | Sumitomo Electric Industries | |
| DE2538313C3 (en) * | 1975-08-28 | 1981-11-05 | Heraeus Quarzschmelze Gmbh, 6450 Hanau | Process for the production of a preliminary product for the production of an optical, self-focusing light guide |
| US4339173A (en) * | 1975-09-08 | 1982-07-13 | Corning Glass Works | Optical waveguide containing P2 O5 and GeO2 |
| DE2546162B1 (en) * | 1975-10-15 | 1976-09-23 | Jenaer Glaswerk Schott & Gen | Optical fiber with a refractive index gradient for communication |
| AU504423B2 (en) * | 1975-11-14 | 1979-10-11 | International Standard Electric Corporation | Optical fibre |
| JPS5621777Y2 (en) * | 1976-02-04 | 1981-05-22 | ||
| DE2614183C3 (en) * | 1976-04-02 | 1981-11-12 | Jenaer Glaswerk Schott & Gen., 6500 Mainz | Optical fiber with gradient profile of the refractive index, low transmission losses, high transmission capacity and large aperature when using GeO ↓ 2 ↓ |
| JPS5838367B2 (en) * | 1976-04-24 | 1983-08-23 | 株式会社フジクラ | Method of manufacturing optical transmission fiber |
| JPS5838368B2 (en) * | 1976-05-15 | 1983-08-23 | 住友電気工業株式会社 | Optical fiber manufacturing method |
| JPS52153750A (en) * | 1976-06-17 | 1977-12-21 | Fujitsu Ltd | Production of optical transmission wire |
| GB1586119A (en) * | 1976-07-05 | 1981-03-18 | Fujitsu Ltd | Method of producing an optical fibre preform |
| DE2642949C3 (en) * | 1976-09-24 | 1980-11-20 | Philips Patentverwaltung Gmbh, 2000 Hamburg | Process for the production of internally coated glass tubes for drawing optical fibers |
| US4111525A (en) * | 1976-10-12 | 1978-09-05 | Bell Telephone Laboratories, Incorporated | Silica based optical fiber waveguide using phosphorus pentoxide and germanium dioxide |
| JPS5395649A (en) * | 1977-02-02 | 1978-08-22 | Hitachi Ltd | Production of optical fiber |
| CA1080562A (en) * | 1977-02-10 | 1980-07-01 | Frederick D. King | Method of and apparatus for manufacturing an optical fibre with plasma activated deposition in a tube |
| GB1602052A (en) * | 1977-06-20 | 1981-11-04 | Int Standard Electric Corp | Optical fibre manufacture |
| DE2814380C3 (en) * | 1978-04-04 | 1982-07-08 | Schott Glaswerke, 6500 Mainz | Process for the production of optical glass fibers from a collapsed silica glass tube |
| US4229070A (en) * | 1978-07-31 | 1980-10-21 | Corning Glass Works | High bandwidth optical waveguide having B2 O3 free core and method of fabrication |
| US4230396A (en) * | 1978-07-31 | 1980-10-28 | Corning Glass Works | High bandwidth optical waveguides and method of fabrication |
| US4257797A (en) | 1979-01-05 | 1981-03-24 | Western Electric | Optical fiber fabrication process |
| CA1139621A (en) * | 1979-01-05 | 1983-01-18 | Matthew J. Andrejco | Optical fiber fabrication process |
| JPS55104941A (en) * | 1979-02-06 | 1980-08-11 | Nippon Telegr & Teleph Corp <Ntt> | Production of preform for optical fiber |
| DE2929166A1 (en) * | 1979-07-19 | 1981-01-29 | Philips Patentverwaltung | METHOD FOR THE PRODUCTION OF OPTICAL FIBERS |
| US4292422A (en) * | 1979-12-03 | 1981-09-29 | Dow Corning Corporation | Oxygen-curable mercapto-functional organosilicon-organic compound compositions catalyzed by metal carbonyl compounds and method of forming higher molecular weight products therefrom |
| US4425146A (en) * | 1979-12-17 | 1984-01-10 | Nippon Telegraph & Telephone Public Corporation | Method of making glass waveguide for optical circuit |
| GB2071644B (en) * | 1980-02-22 | 1984-03-14 | Sumitomo Electric Industries | Radiation resistant optical fibres and a process for the production thereof |
| US4298364A (en) * | 1980-03-17 | 1981-11-03 | Corning Glass Works | Method of making optical fibers having improved core roundness |
| DE3133013A1 (en) * | 1980-08-26 | 1982-04-08 | Western Electric Co., Inc., 10038 New York, N.Y. | "METHOD FOR PRODUCING A LIGHT-FIBER FIBER BLANK" |
| FR2543455B1 (en) * | 1983-03-30 | 1987-03-27 | Air Liquide | PROCESS FOR OPALIZING THE INTERIOR SURFACE OF OBJECTS OF LONG LENGTH IN RELATION TO THEIR SECTION |
| DE3335126A1 (en) * | 1983-09-28 | 1985-04-11 | Wacker-Chemitronic Gesellschaft für Elektronik-Grundstoffe mbH, 8263 Burghausen | METHOD FOR CHEMICAL GAS PHASE DEPOSITION OF OXIDIC PARTICLES |
| JPH04135612U (en) * | 1991-06-11 | 1992-12-17 | ナシヨナル住宅産業株式会社 | Exterior wall panel joint structure |
| KR0153835B1 (en) * | 1995-11-07 | 1998-11-16 | 김광호 | Process for preparation of optical glass fiber |
| US6769275B2 (en) * | 2002-03-15 | 2004-08-03 | Fibercore, Inc. | Method for making optical fiber preform using simultaneous inside and outside deposition |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3737293A (en) * | 1972-01-03 | 1973-06-05 | Corning Glass Works | Method of forming an economic optical waveguide fiber |
| JPS4886918A (en) * | 1972-02-22 | 1973-11-16 | ||
| GB1427327A (en) * | 1972-06-08 | 1976-03-10 | Standard Telephones Cables Ltd | Glass optical fibres |
| DE2434717C2 (en) * | 1973-08-21 | 1989-05-18 | International Standard Electric Corp., 10022 New York, N.Y. | Method of manufacturing a fiber optic light guide |
| JPS59454B2 (en) * | 1973-09-22 | 1984-01-06 | 住友電気工業株式会社 | Manufacturing method of fiber base material for optical transmission |
-
1975
- 1975-02-07 CA CA219,629A patent/CA1050833A/en not_active Expired
- 1975-02-19 GB GB709275A patent/GB1500530A/en not_active Expired
- 1975-02-20 DE DE19752507340 patent/DE2507340B2/en not_active Ceased
- 1975-02-20 NL NL7502017A patent/NL165720C/en not_active IP Right Cessation
- 1975-02-21 FR FR7505480A patent/FR2261992B1/fr not_active Expired
- 1975-02-22 JP JP2147175A patent/JPS5522423B2/ja not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| NL165720B (en) | 1980-12-15 |
| FR2261992A1 (en) | 1975-09-19 |
| NL7502017A (en) | 1975-08-26 |
| DE2507340B2 (en) | 1979-03-01 |
| NL165720C (en) | 1984-02-16 |
| JPS5522423B2 (en) | 1980-06-17 |
| DE2507340A1 (en) | 1975-08-28 |
| FR2261992B1 (en) | 1980-01-04 |
| JPS50120352A (en) | 1975-09-20 |
| GB1500530A (en) | 1978-02-08 |
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