CN109081911A - A kind of polyester production device that stablizing dyeing and its production technology - Google Patents
A kind of polyester production device that stablizing dyeing and its production technology Download PDFInfo
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- CN109081911A CN109081911A CN201810755290.9A CN201810755290A CN109081911A CN 109081911 A CN109081911 A CN 109081911A CN 201810755290 A CN201810755290 A CN 201810755290A CN 109081911 A CN109081911 A CN 109081911A
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- Prior art keywords
- diethylene glycol
- esterification
- reaction kettle
- temperature
- pressure
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/78—Preparation processes
- C08G63/785—Preparation processes characterised by the apparatus used
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
- C08G63/00—Macromolecular compounds obtained by reactions forming a carboxylic ester link in the main chain of the macromolecule
- C08G63/66—Polyesters containing oxygen in the form of ether groups
- C08G63/668—Polyesters containing oxygen in the form of ether groups derived from polycarboxylic acids and polyhydroxy compounds
- C08G63/672—Dicarboxylic acids and dihydroxy compounds
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- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Polyesters Or Polycarbonates (AREA)
Abstract
The invention discloses polyester production devices and its production technology that one kind can stablize dyeing, including slurry tank, the first reaction kettle of the esterification, the second reaction kettle of the esterification, prepolymerization reaction kettle, the second batch condensation polymerization reactor and the final polycondensation reaction kettle being successively equipped with, it further include diethylene glycol (DEG) storage tank, plunger pump and flowmeter, diethylene glycol (DEG) storage tank is connect by delivery pipe with flowmeter, flowmeter is connect with slurry tank, plunger pump setting is additionally provided with the logical control valve only of control diethylene glycol (DEG) in delivery pipe, in delivery pipe.The polyester production device that dyeing can be stablized promotes slice dye stability by diethylene glycol (DEG) concentration in control slice.
Description
Technical field:
The present invention relates to dacron thread production fields, are especially a kind of polyester production device and its production that can stablize dyeing
Technique.
Background technique:
In polyethylene terephthalate production process, the change of the factors such as raw materials for production, produce load, technological parameter
Change, such as controls the improper dyeing uniformity that can seriously affect fiber, have a significant impact to rear road dyeing process.To spin dyeing work
For skill, it is sliced the stability of dyeing, stainability is always sliced a great problem spun, dyeing unevenness, the increase of substandard products cloth, waste
Seriously.
Summary of the invention:
The technical problem to be solved by the invention is to provide diethylene glycol (DEG) concentration in a kind of control slice to promote slice dyeing surely
The polyester production device of dyeing can qualitatively be stablized, be sliced when road dyeing process after the slice satisfaction slice of process units production
Dying-stable, uniformly, stainability is good.
The technical solution of the invention is as follows, provides a kind of polyethylene terephthalate production dress that can stablize dyeing
It sets, including slurry tank, the first reaction kettle of the esterification, the second reaction kettle of the esterification, the prepolymerization reaction kettle, the second contracting being successively equipped with
Poly- reaction kettle and final polycondensation reaction kettle, further include diethylene glycol (DEG) storage tank, plunger pump and flowmeter, diethylene glycol (DEG) storage tank by delivery pipe with
Flowmeter connection, flowmeter are connect with slurry tank, and it is logical that plunger pump setting is additionally provided with control diethylene glycol (DEG) in delivery pipe, in delivery pipe
Control valve only.
Preferably, control valve includes the first ball valve being successively set in delivery pipe along diethylene glycol (DEG) conveying direction, Y type mistake
Trap valve, check-valves and the second ball valve.
The present invention also provides the production technologies that one kind can stablize the polyester production device of dyeing, by increasing by one for storing up
A certain amount of diethylene glycol solution is added in slurry tank by the stainless steel storage tank for depositing diethylene glycol solution, with p-phthalic acid and
Ethylene glycol is mixed into suspension, is transported to the first reaction kettle of the esterification by delivery pump, under the pressure of 66-72KPa and 256-266
The first esterification is carried out at a temperature of DEG C, second reaction kettle of the esterification is flowed to by potential difference after the first esterification is good, in 18-
Under the pressure of 23KPa and the second esterification is carried out at a temperature of 260-270 DEG C or so, precondensation is arrived after the second esterification is good
Reaction, under the pressure of 8-12KPa and 265-275 DEG C at a temperature of carry out first polycondensation reaction, by potential difference inflow second
Batch condensation polymerization reactor, under the pressure of 1-2KPa and 272-283 DEG C at a temperature of carry out the second polycondensation reaction, finally in 0.06-
Under the pressure of 0.2KPa and final polycondensation reaction is carried out at a temperature of 275-285 DEG C, melt is made into poly- pair by pelleter system
Ethylene terephthalate makes the diethylene glycol content in finished product reach 1.1-2.1%.
Further, diethylene glycol solution adds 25-60kg into slurry tank per hour.
It further, will be a certain amount of by increasing the stainless steel storage tank of 5 tons of capacity for storing diethylene glycol solution
Diethylene glycol solution be added in slurry tank, be mixed into suspension with p-phthalic acid and ethylene glycol, conveyed by delivery pump
To the first reaction kettle of the esterification, under the pressure of 70KPa and 262 DEG C at a temperature of carry out the first esterification, the first esterification
Second reaction kettle of the esterification is flowed to by potential difference after good, at a temperature of the second esterification of progress under the pressure of 20KPa with 266 DEG C or so
Reaction, after the second esterification is good arrive prepolymerization reaction, under the pressure of 10KPa with 271 DEG C at a temperature of carry out the first polycondensation
Reaction, by potential difference flow into the second batch condensation polymerization reactor, under the pressure of 1.5KPa with 279 DEG C at a temperature of carry out the second polycondensation
Reaction, finally under the pressure of 0.1KPa and 280 DEG C at a temperature of carry out final polycondensation reaction, melt is done by pelleter system
At polyethylene terephthalate, the diethylene glycol content in finished product is made to reach 1.56%.
Using after above scheme compared with prior art, the invention has the following advantages that due in actual production to cutting
Discovery is tested in piece sampling analysis, and causing the uneven main physical index of slice dyeing is that the concentration of slice diethylene glycol content does not conform to
It is suitable, by diethylene glycol content caused by itself, containing in finished product in the esterifying polycondensation production process of existing process units
Measure relatively low, be not achieved good dyeability and chromatophilia, thus by additional diethylene glycol (DEG) control slice diethylene glycol content it is dense
Degree is particularly important to post-processing dyeing, and uniformity, the chromatophilia of road dyeing process generation, subtract after the stable satisfaction of requirements at the higher level
The wasting of resources and artificial waste that few dyeing is uneven and generates.
Detailed description of the invention:
Fig. 1 is the structural diagram of the present invention.
Specific embodiment:
With regard to specific embodiment, the invention will be further described below:
It is analyzed and is tested according to Slice Sampling, slice dyeing is unstable, uneven, and chromatophilia difference is mainly sliced diethylene glycol (DEG) and contains
Caused by the concentration of amount, although and existing pet reaction production equipment in esterifying polycondensation production process two caused by itself
Glycol content, but its content in finished product only has 0.7-0.9%, is unable to satisfy the requirement for stablizing dyeing.So the present invention mentions
The polyester production device of dyeing can be stablized for one kind, as shown in Figure 1, including the slurry tank for passing sequentially through transfer pipeline connection setting
1, the first reaction kettle of the esterification 2, the second reaction kettle of the esterification 3, prepolymerization reaction kettle 4, the second batch condensation polymerization reactor 5 and final polycondensation reaction kettle
6, pelleter 7 is connected behind reaction kettle 6, further includes diethylene glycol (DEG) storage tank 8, plunger pump 9 and flowmeter 10, diethylene glycol (DEG) storage tank 8 passes through
Delivery pipe is connect with flowmeter 10, and flowmeter 10 is connect with slurry tank 1, and plunger pump 9 is arranged in delivery pipe, is also set in delivery pipe
There is the logical control valve only of control diethylene glycol (DEG).Wherein, in order to optimize structure, control valve includes setting gradually along diethylene glycol (DEG) conveying direction
The first ball valve 11, Y type strainer valve 12, check-valves 13 and the second ball valve 14 in delivery pipe, wherein the first ball valve 11, Y type mistake
Trap valve 12 is located in the delivery pipe of 9 two sides of plunger pump with check-valves 13 and the second ball valve 14 to be arranged.Pass through additional diethylene glycol (DEG)
Solution increases an independent diethylene glycol (DEG) storage tank, and by transformation, a certain amount of diethylene glycol solution is added in slurry tank, from
The first esterification is identified oneself at the very start, the second esterification, precondensation, the second polycondensation, arrives final polycondensation reaction, will finally be sliced diethylene glycol (DEG)
Content is increased to required content.
Specific production technology is as follows, (raw according to day by increasing a stainless steel storage tank for storing diethylene glycol solution
400 tons of device capbility is produced, the capacity matching of the storage tank is at 5 tons), a certain amount of diethylene glycol solution is added in slurry tank,
Cooperate also plunger pump and the flowmeter of storage tank, diethylene glycol (DEG) tank is connect by delivery pipe with flowmeter, and flowmeter and slurry pipe connect
It connects, plunger pump setting is additionally provided with the be successively set in delivery pipe along diethylene glycol (DEG) conveying direction in delivery pipe, in delivery pipe
One ball valve, Y type strainer valve, check-valves and the second ball valve.Specifically, adding 25-60kg diethylene glycol solution into slurry tank per hour
It is mixed into suspension with p-phthalic acid and ethylene glycol, the first reaction kettle of the esterification is transported to by delivery pump, in the pressure of 70KPa
Under power and the first esterification is carried out at a temperature of 262 DEG C, diethylene glycol content can achieve 1.2% at this time.First esterification
Second reaction kettle of the esterification is flowed to by potential difference after good, at a temperature of the second esterification of progress under the pressure of 20KPa with 266 DEG C is anti-
It answers, diethylene glycol content can achieve 1.45%.Prepolymerization reaction is arrived after second esterification is good, under the pressure of 10KPa or so
First polycondensation reaction is carried out at a temperature of with 271 DEG C or so, the second batch condensation polymerization reactor is being flowed by potential difference, in the pressure of 1.5KPa
Under power and the second polycondensation reaction is carried out at a temperature of 279 DEG C, finally the at a temperature of progress under the pressure of 0.1KPa with 280 DEG C is whole
Melt is made into polyethylene terephthalate by pelleter system, reaches the diethylene glycol content in finished product by polycondensation reaction
It to reasonable content, is found according to testing, value selects 1.56% preferably, its dyeing effect of the slice of this content is stable and equal
Even, stainability is good.
In addition, increasing the assay of slice diethylene glycol (DEG) to monitor slice diethylene glycol content, by every four days one original
It is secondary, it is changed to every two days one time assay, monitors the stabilization of slice diethylene glycol content.Periodically switching diethylene glycol (DEG) pump, by each
Moon switching is primary, it is ensured that the flow of pump.Y-type filter before periodic cleaning diethylene glycol (DEG) pump, it is primary by cleaning every month, it is ensured that pump
Normal operation.And reinforce the monitoring of daily management, the every inspection in two hours of Field Force, it is ensured that the normal fortune of diethylene glycol (DEG) pump
Row.
Only the preferred embodiment of the present invention has been described above, but is not to be construed as limiting the scope of the invention.It is all
The equivalent structure or equivalent flow shift done using description of the invention, be included in scope of patent protection of the invention it
It is interior.
Claims (5)
1. one kind can stablize the polyethylene terephthalate process units of dyeing, including be successively equipped with slurry tank,
First reaction kettle of the esterification, the second reaction kettle of the esterification, prepolymerization reaction kettle, the second batch condensation polymerization reactor and final polycondensation reaction kettle, it is special
Sign is: further including diethylene glycol (DEG) storage tank, plunger pump and flowmeter, diethylene glycol (DEG) storage tank is connect by delivery pipe with flowmeter, flow
Meter is connect with slurry tank, and plunger pump setting is additionally provided with the logical control valve only of control diethylene glycol (DEG) in delivery pipe, in delivery pipe.
2. the polyethylene terephthalate process units according to claim 1 for stablizing dyeing, it is characterised in that:
Control valve includes the first ball valve being successively set in delivery pipe along diethylene glycol (DEG) conveying direction, Y type strainer valve, check-valves and second
Ball valve.
3. the production technology that one kind can stablize the polyethylene terephthalate process units of dyeing, it is characterised in that: pass through
Increase the stainless steel storage tank for being used to store diethylene glycol solution, a certain amount of diethylene glycol solution is added in slurry tank, with
P-phthalic acid and ethylene glycol are mixed into suspension, the first reaction kettle of the esterification are transported to by delivery pump, 66-72KPa's
Under pressure and the first esterification is carried out at a temperature of 256-266 DEG C, second ester is flowed to by potential difference after the first esterification is good
Change reaction kettle, under the pressure of 18-23KPa and 260-270 DEG C or so at a temperature of carry out the second esterification, the second esterification is anti-
Ying Haohou to prepolymerization reaction, under the pressure of 8-12KPa and 265-275 DEG C at a temperature of carry out first polycondensation reaction, logical
Cross potential difference flow into the second batch condensation polymerization reactor, under the pressure of 1-2KPa and 272-283 DEG C at a temperature of carry out the second polycondensation reaction,
Finally under the pressure of 0.06-0.2KPa and 275-285 DEG C at a temperature of carry out final polycondensation reaction, will be melted by pelleter system
Body is made into polyethylene terephthalate, and the diethylene glycol content in finished product is made to reach 1.1-2.1%.
4. according to the production technology for the polyethylene terephthalate process units for stablizing dyeing that claim 3 is stated,
Be characterized in that: diethylene glycol solution adds 25-60kg into slurry tank per hour.
5. according to the production technology for the polyethylene terephthalate process units for stablizing dyeing that claim 3 is stated,
It is characterized by the stainless steel storage tank for increasing by 5 tons of capacity for storing diethylene glycol solution, by a certain amount of diethylene glycol (DEG)
Solution is added in slurry tank, is mixed into suspension with p-phthalic acid and ethylene glycol, is transported to the first ester by delivery pump
Change reaction kettle, under the pressure of 70KPa and 262 DEG C at a temperature of carry out the first esterification, pass through after the first esterification is good
Potential difference flows to the second reaction kettle of the esterification, under the pressure of 20KPa and 266 DEG C or so at a temperature of carry out the second esterification, the
It is class it is completely reacted after arrive prepolymerization reaction, under the pressure of 10KPa and 271 DEG C at a temperature of carry out first polycondensation reaction,
By potential difference flow into the second batch condensation polymerization reactor, under the pressure of 1.5KPa and 279 DEG C at a temperature of carry out the second polycondensation reaction, most
Afterwards under the pressure of 0.1KPa and 280 DEG C at a temperature of carry out final polycondensation reaction, melt is made into poly- pair by pelleter system
Ethylene terephthalate makes the diethylene glycol content in finished product reach 1.56%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810755290.9A CN109081911A (en) | 2018-07-11 | 2018-07-11 | A kind of polyester production device that stablizing dyeing and its production technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810755290.9A CN109081911A (en) | 2018-07-11 | 2018-07-11 | A kind of polyester production device that stablizing dyeing and its production technology |
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| Publication Number | Publication Date |
|---|---|
| CN109081911A true CN109081911A (en) | 2018-12-25 |
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ID=64837590
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810755290.9A Pending CN109081911A (en) | 2018-07-11 | 2018-07-11 | A kind of polyester production device that stablizing dyeing and its production technology |
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| Country | Link |
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| CN (1) | CN109081911A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115340670A (en) * | 2022-09-21 | 2022-11-15 | 湖北绿宇环保有限公司 | Production process of polyester chip special for non-woven fabric |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644600A (en) * | 2004-09-01 | 2005-07-27 | 薛纪良 | Preparation of polyethylene glycol terephthalate for improving color value of product |
| CN103304791A (en) * | 2013-05-08 | 2013-09-18 | 江苏德力化纤有限公司 | Preparation process of high-quality fusant |
| CN203346318U (en) * | 2013-06-03 | 2013-12-18 | 扬州惠通化工技术有限公司 | Production device for polyester melt with waste bottle chip |
-
2018
- 2018-07-11 CN CN201810755290.9A patent/CN109081911A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1644600A (en) * | 2004-09-01 | 2005-07-27 | 薛纪良 | Preparation of polyethylene glycol terephthalate for improving color value of product |
| CN103304791A (en) * | 2013-05-08 | 2013-09-18 | 江苏德力化纤有限公司 | Preparation process of high-quality fusant |
| CN203346318U (en) * | 2013-06-03 | 2013-12-18 | 扬州惠通化工技术有限公司 | Production device for polyester melt with waste bottle chip |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115340670A (en) * | 2022-09-21 | 2022-11-15 | 湖北绿宇环保有限公司 | Production process of polyester chip special for non-woven fabric |
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