Patent US4448736A successfully refreshed from Google Patents.
US4448736A
Expired / Lapsed
US
⏱️ 0.0 years remaining
Continuous in-line melt flow rate control system
Assignee: BP Corp North America Inc
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Filing: 1982-05-24
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Granted: 1984-05-15
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Expires: 2002-05-24
Abstract
Abstract The continuous in-line melt flow rate control system (40; 100) is coupled to a mixer/extruder system (10; 97) including a polymer, stabilizer and degradent feeding system (12, 16, 18; 102) supplying mixed materials to the inlet end of an extruder (24; 108) having a die head (26) at the outlet end thereof. The control system (40; 100) is coupled between a rheometer (42; 112) which monitors a slip stream (46; 110) of melt from the extruder (24; 108) and a ratio controller (48; 93) in the feeding system (12, 16, 18; 102). The control system (40; 100) includes a rheometer (42; 112) which monitors the viscosity of the slip stream of melt from the extruder (24; 108) upstream from the die head (26) and converts the monitored viscosity value to a process signal (F) and a controller (44; 84; 101) that compares the process signal (F) with a set point value (A) related to a target melt flow rate and generates a correction signal (B, C, D) when there is a difference between the process signal (F) and the set point value (A). The correction signal (D) is supplied to the degradent ratio controller (48; 93) for adjusting the amount of degradent added to the polymer fed to the extruder (24; 108) in response to the deviation of the process signal (F) from the set point value (A).
Inventors
- 👤 Donald B. Emery
- 👤 William M. Herring
Bibliographic Details
Application Number
—
Jurisdiction
US
Data Source
google_patents
Last Synchronized
2026-10-26 21:19
CPC Classifications
B; B29; B29C; B29C48/00; B29C48/25; B29C48/92; B29B; B29B7/00; B29B7/30; B29B7/34; B29B7/38; B29B7/58; B29B7/60; B29B7/603; B29B7/72; B29B7/726; B29B7/728; B29B7/74; B29B7/7461; B29B7/7476; B29B7/7485; B29B7/80; B29B7/88; B29B9/00; B29B9/02; B29B9/06; B29C2948/00; B29C2948/92; B29C2948/92009; B29C2948/92085; B29C2948/92104; B29C2948/922; B29C2948/92504; B29C2948/9258; B29C2948/926; B29C2948/92695; B29C2948/92819; B29C2948/92857; B29C2948/92876; B29C2948/92904; B29C48/03; B29C48/05; B29C48/07; B29C48/08
Claims Analysis
Total Claims: 30
Claim 1
Independent Claim
260 words
A method for controlling the molecular weight of a polymer being extruded through a die head at the outlet end of an extruder by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said method comprising the steps of: monitoring the viscosity of a slip stream of melt from the extruder upstream from the die head; converting the monitored viscosity value to a process signal; comparing the process signal with a set point value related to a target melt flow rate; generating a correction signal when there is a difference between the process signal and the set point value; supplying said correction signal to a degradent additive feed control system for adjusting the amount of degradent added to the polymer fed to the extruder in response to the deviation of the process signal from the set point value; comparing the actual process signal with an approximated process model signal which includes at least one model for the process transition and a model for dead time; after the process transition and dead time periods have completely reacted to the correction signal, comparing the process signal with the set point value and if there is still a difference between the process signal and the set point value, generating a further correction signal and repeating the above thereby to maintain the melt flow rate as closely as possible to a target melt flow rate related to the desired polymer molecular weight.
Claim 2
Independent Claim
260 words
A method for controlling the molecular weight of a polymer being extruded through a die head at the outlet end of an extruder by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said method comprising the steps of: monitoring the viscosity of a slip stream of melt from the extruder upstream from the die head; converting the monitored viscosity value to a process signal; comparing the process signal with a set point value related to a target melt flow rate; generating a correction signal when there is a difference between the process signal and the set point value; supplying said correction signal to a degradent additive feed control system for adjusting the amount of degradent added to the polymer fed to the extruder in response to the deviation of the process signal from the set point value; comparing the actual process signal with an approximated process model signal which includes at least one model for the process transition and a model for dead time; after the process transition and dead time periods have completely reacted to the correction signal, comparing the process signal with the set point value and if there is still a difference between the process signal and the set point value, generating a further correction signal and repeating the above thereby to maintain the melt flow rate as closely as possible to a target melt flow rate related to the desired polymer molecular weight.
Claim 3
Dependent Claim
20 words
The method of claim 1 wherein said process model signal includes a first process model and a second process model.
Claim 4
Dependent Claim
24 words
The method of claim 1 wherein said process model signal has a dead time of a few minutes up to 45 minutes or more.
Claim 5
Dependent Claim
38 words
The method of claim 1 wherein said degradent additive control system includes a feed forward control system including a polymer feed controller and a slave ratio controller for controlling the ratio of degradent mixed with the polymer feed.
Claim 6
Dependent Claim
46 words
The method of claim 1 including the further step of immediately comparing the correction signal with a predetermined process signal from the process transition model to indicate that a correction has been effected prior to the time the actual correction works its way through the extruder.
Claim 7
Independent Claim
242 words
A method for continuously controlling the molecular weight of a polymer exiting a polymer mixing and extruding system by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said method comprising the steps of: monitoring the viscosity of a slip stream of melt from the extruder upstream of an extruder die head with a rheometer having a positive pressure displacement pump; sensing a difference in the rheometer pump speed from the pump speed required to maintain a desired rate of flow of polymer at constant temperature and pressure through an orifice; altering the amount of degradent added to the polymer supplied to the mixing and extruding system in response to the sensed difference in speed of the pump; subsequently comparing the pump speed to the pump speed value required to maintain the desired rate of flow of the polymer at a constant temperature and pressure through an orifice after the altered ratio mixture of polymer and degradent has worked its way through the mixing and extruding system; and, if a difference in pump speed is sensed, repeating the above until the rate of flow of polymer at constant temperature and pressure through an orifice is substantially the desired rate of flow of polymer at constant temperature and pressure through an orifice related to the desired molecular weight of the polymer.
Claim 8
Independent Claim
242 words
A method for continuously controlling the molecular weight of a polymer exiting a polymer mixing and extruding system by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said method comprising the steps of: monitoring the viscosity of a slip stream of melt from the extruder upstream of an extruder die head with a rheometer having a positive pressure displacement pump; sensing a difference in the rheometer pump speed from the pump speed required to maintain a desired rate of flow of polymer at constant temperature and pressure through an orifice; altering the amount of degradent added to the polymer supplied to the mixing and extruding system in response to the sensed difference in speed of the pump; subsequently comparing the pump speed to the pump speed value required to maintain the desired rate of flow of the polymer at a constant temperature and pressure through an orifice after the altered ratio mixture of polymer and degradent has worked its way through the mixing and extruding system; and, if a difference in pump speed is sensed, repeating the above until the rate of flow of polymer at constant temperature and pressure through an orifice is substantially the desired rate of flow of polymer at constant temperature and pressure through an orifice related to the desired molecular weight of the polymer.
Claim 9
Dependent Claim
87 words
The method of claim 6 wherein said step of subsequently comparing the actual pump speed to a pump speed value which, for a constant temperature and pressure in the rheometer, will provide a desired melt flow rate includes the step of comparing the instantaneous pump speed and subsequent changing pump speed after the altered ratio mixture of polymer and degradent work through the mixing and extruding system to a process model signal for pump speed which includes at least one process model and a dead time model.
Claim 10
Dependent Claim
19 words
The method of claim 7 wherein said process model signal for pump speed includes first and second process models.
Claim 11
Dependent Claim
58 words
The method of claim 7 including the further step of immediately comparing the process model signal for the transition in pump speed with a correction signal used to alter the addition of degradent thereby to indicate that a correction has been effected prior to the time the actual correction works its way through the mixing and extruding system.
Claim 12
Independent Claim
273 words
An apparatus for controlling the molecular weight of the polymer being extruded through a die head at the outlet of an extruder by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said apparatus comprising: means for monitoring the viscosity of a slip stream of melt from the extruder upstream of the die head; means for converting the monitored viscosity value to a process signal; means for comparing the process signal with a set point value related to a target melt flow rate; means for generating a correction signal when there is a difference between the process signal and the set point value; means for supplying said correction signal to a degradent additive feed control system for adjusting the amount of degradent added to the polymer fed to the extruder in response to the deviation of the process signal from the set point value; means for comparing the actual process signal with an approximated process model signal which includes at least one model for the process transition and a model for dead time; means for comparing the process signal with the set point value after the process transition and dead time periods have elapsed and a steady state condition has been reached, and if there is still a difference between the process signal and the set point value, said apparatus being operable to generate a further correction signal thereby to maintain the melt flow rate as close as possible to the target melt flow related to the desired polymer molecular weight.
Claim 13
Independent Claim
273 words
An apparatus for controlling the molecular weight of the polymer being extruded through a die head at the outlet of an extruder by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said apparatus comprising: means for monitoring the viscosity of a slip stream of melt from the extruder upstream of the die head; means for converting the monitored viscosity value to a process signal; means for comparing the process signal with a set point value related to a target melt flow rate; means for generating a correction signal when there is a difference between the process signal and the set point value; means for supplying said correction signal to a degradent additive feed control system for adjusting the amount of degradent added to the polymer fed to the extruder in response to the deviation of the process signal from the set point value; means for comparing the actual process signal with an approximated process model signal which includes at least one model for the process transition and a model for dead time; means for comparing the process signal with the set point value after the process transition and dead time periods have elapsed and a steady state condition has been reached, and if there is still a difference between the process signal and the set point value, said apparatus being operable to generate a further correction signal thereby to maintain the melt flow rate as close as possible to the target melt flow related to the desired polymer molecular weight.
Claim 14
Dependent Claim
20 words
The apparatus of claim 10 wherein said process model signal includes a first process model and a second process model.
Claim 15
Dependent Claim
39 words
The apparatus of claim 10 wherein said degradent additive feed control system includes a feed forward control system including a polymer feed controller and a slave ratio controller for controlling the ratio of degradent mixed with the polymer feed.
Claim 16
Dependent Claim
209 words
Apparatus for continuously controlling the molecular weight of a polymer exiting a polymer mixing and extruding system by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said apparatus comprising: means for monitoring the viscosity of a slip stream of melt from an extruder upstream of an extruder die head, said monitoring means including a rheometer having a positive pressure displacement pump; means for sensing a difference in the rheometer pump speed from the pump speed required to maintain a desired rate of flow of polymer at constant temperature and pressure through an orifice; means for altering the amount of degradent added to the polymer supplied to the mixing and extruding system in response to the sensed difference in speed of the pump and means for subsequently comparing the pump speed to the pump speed value required to maintain the desired rate of flow polymer at a constant temperature and pressure through an orifice after the altered ratio mixture of polymer and degradent has worked its way through the mixing and extruding system and for generating a correction signal if a difference in pump speed is sensed.
Claim 17
Dependent Claim
209 words
Apparatus for continuously controlling the molecular weight of a polymer exiting a polymer mixing and extruding system by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said apparatus comprising: means for monitoring the viscosity of a slip stream of melt from an extruder upstream of an extruder die head, said monitoring means including a rheometer having a positive pressure displacement pump; means for sensing a difference in the rheometer pump speed from the pump speed required to maintain a desired rate of flow of polymer at constant temperature and pressure through an orifice; means for altering the amount of degradent added to the polymer supplied to the mixing and extruding system in response to the sensed difference in speed of the pump and means for subsequently comparing the pump speed to the pump speed value required to maintain the desired rate of flow polymer at a constant temperature and pressure through an orifice after the altered ratio mixture of polymer and degradent has worked its way through the mixing and extruding system and for generating a correction signal if a difference in pump speed is sensed.
Claim 18
Dependent Claim
97 words
The apparatus of claim 13 wherein said comparing means for comparing the actual pump speed to a pump speed value which, for a constant temperature and pressure in the rheometer, will provide a desired melt flow rate, includes means for generating a process model signal for pump speed including at least one process model and a dead time model and said comparing means being operable to compare the instantaneous pump speed and subsequent changing pump speed after the altered ratio mixture of polymer and degradent work through the mixing and extruding system to said process model signal.
Claim 19
Dependent Claim
19 words
The apparatus of claim 14 wherein said process model signal for pump speed includes first and second process models.
Claim 20
Dependent Claim
203 words
A mixing and extruding system for controlling the molecular weight of a polymer being extruded by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said system including an extruder having an inlet for receiving a mixture of polymer, stabilizer and degradent for being extruded through a die head at the outlet end of said extruder, mixing means for mixing polymer, stabilizer and degradent prior to feeding same into the inlet end of said extruder, feeding means for feeding polymer, stabilizer and degradent in predetermined ratios to said mixing means and including ratio altering means, a rheometer, a slip stream conduit connection to said extruder upstream from said die head for supplying a stream of melt from said extruder to said rheometer, control means coupled to said rheometer and to said ratio altering means and including means for comparing the melt flow rate sensed by said rheometer to a target melt flow rate related to the desired polymer molecular weight and for altering the ratio in response to a change in the melt flow rate from the target melt flow rate.
Claim 21
Dependent Claim
203 words
A mixing and extruding system for controlling the molecular weight of a polymer being extruded by altering, in a forward control manner, the mixture of degradent and polymer fed to the extruder relative to a target melt flow rate related to the molecular weight of polymer desired, said system including an extruder having an inlet for receiving a mixture of polymer, stabilizer and degradent for being extruded through a die head at the outlet end of said extruder, mixing means for mixing polymer, stabilizer and degradent prior to feeding same into the inlet end of said extruder, feeding means for feeding polymer, stabilizer and degradent in predetermined ratios to said mixing means and including ratio altering means, a rheometer, a slip stream conduit connection to said extruder upstream from said die head for supplying a stream of melt from said extruder to said rheometer, control means coupled to said rheometer and to said ratio altering means and including means for comparing the melt flow rate sensed by said rheometer to a target melt flow rate related to the desired polymer molecular weight and for altering the ratio in response to a change in the melt flow rate from the target melt flow rate.
Claim 22
Dependent Claim
130 words
The system of claim 16 wherein said rheometer is operable to maintain a substantially constant pressure and temperature at an outlet orifice thereof with the pump speed of a rheometer-positive-displacement pump varying in response to changes in viscosity of the melt and said control means including means for sensing the speed of said pump and for comparing said pump speed with a target pump speed which in conjunction with the constant temperature and pressure provides the desired melt flow rate, and said comparing means being operable to cause the ratio of said ratio altering means to be altered in response to a deviation in pump speed from the target pump speed to cause the pump speed to return to the target pump speed to produce the desired melt flow rate.
Claim 23
Dependent Claim
55 words
The system of claim 17 wherein said control means include a computer and said computer is programmed to compare the change in pump speed after the ratio of degradent to polymer has been altered, to a process model signal for the pump speed response including at least one process model and one dead time model.
Claim 24
Dependent Claim
21 words
The system of claim 18 wherein said process model signal includes first and second process models and the dead time model.
Claim 25
Dependent Claim
15 words
The system of claim 16 wherein said mixing means include first and second mixing apparatus.
Claim 26
Dependent Claim
142 words
The system of claim 16 wherein said mixing means include a feed forward control system for supplying polymer and degradent in a predetermined ratio to said inlet end of said extruder and wherein said control means include a melt flow rate controller coupled between the output of said rheometer and said feed forward control system, means for establishing a set point value related to said target melt flow rate and for supplying same to said melt flow rate controller which is operable to compare the set point value with a value corresponding to the measured melt flow rate and for operating said ratio altering means to cause the ratio of degradent mixed with the polymer to be altered in response to a deviation of the product melt flow rate from a desired melt flow rate as established by the set point value.
Claim 27
Dependent Claim
107 words
The system of claim 21 wherein said feed forward control system includes a feed controller for controlling the feed of polymer to said mixing means and said ratio altering means are defined by a slave ratio controller coupled to said feed controller and to a degradent feeder for controlling the ratio of degradent mixed with said polymer and wherein said melt flow rate controller is coupled to said ratio controller for changing the setting of said ratio controller to alter the ratio of the mixture of degradent and polymer in response to a change in the product melt flow rate as established by the set point value.
Claim 28
Dependent Claim
181 words
The system of claim 22 wherein said melt flow rate controller includes a set point comparator having one input for receiving the set point value and another input for receiving a process signal from the rheometer indicative of the product melt flow rate, a proportional-plus-integral calculator, a set point/process/model comparator having one input coupled to the output of said set point comparator and having an output coupled to said proportional-plus-integral calculator, a process model having an input and an output, the output from said proportional-plus-integral calculator being coupled to said feed forward control system and to the input of said process model, the output of said process model being coupled to the other input of said set point/process/model comparator, a dead time model and a model comparator, the output of said process model being supplied to said dead time model and the process model plus dead time model output signal being supplied to and compared by said model comparator with the actual process signal from said rheometer, and the output of said model comparator being supplied to said set point comparator.
Claim 29
Dependent Claim
18 words
The system of claim 23 including a filter between the output of said rheometer and said model comparator.
Claim 30
Dependent Claim
68 words
The system of claim 23 wherein said process model includes a process one model and a process two model, the output from said proportional-plus-integral calculator being supplied to the inputs of said process one and process two models and the outputs of said process one and process two models being supplied to a summing circuit, the output of said summing circuit being supplied to said dead time model.
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USPTO Annuity & Maintenance Windows
| Annuity Stage | Window Opens | Payment Deadline | Surcharge Period Until | Estimated Fee | Status |
|---|---|---|---|---|---|
| 3.5 Years (Year 4) | 1987-05-15 | 1987-11-14 | 1988-05-15 | $2000.00 | Window Closed / Lapsed |
| 7.5 Years (Year 8) | 1991-05-15 | 1991-11-14 | 1992-05-15 | $3760.00 | Window Closed / Lapsed |
| 11.5 Years (Year 12) | 1995-05-15 | 1995-11-14 | 1996-05-15 | $7700.00 | Window Closed / Lapsed |