CN101250257A - Polymerization esterification residual heat utilization method and apparatus - Google Patents
Polymerization esterification residual heat utilization method and apparatus Download PDFInfo
- Publication number
- CN101250257A CN101250257A CNA2008100612784A CN200810061278A CN101250257A CN 101250257 A CN101250257 A CN 101250257A CN A2008100612784 A CNA2008100612784 A CN A2008100612784A CN 200810061278 A CN200810061278 A CN 200810061278A CN 101250257 A CN101250257 A CN 101250257A
- Authority
- CN
- China
- Prior art keywords
- steam
- esterification
- pipe
- water
- refrigerator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A30/00—Adapting or protecting infrastructure or their operation
- Y02A30/27—Relating to heating, ventilation or air conditioning [HVAC] technologies
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/62—Absorption based systems
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
A utilization method of polymerization esterification residual heat and a device are disclosed. The method is that tower top waste steam of a knockout tower on the upper portion of an esterification reaction kettle is led out and supplied to at least one lithium brominate refrigerator as heat source, a collecting tank is arranged on the outlet of condensed water of the refrigerator, water is transmitted to a waste water collecting tank with a pump, a part of water is used as tower top reflux water, and the rest overflows into a stripping tower to be reclaimed. A pressure regulating valve is added on a pipe which is used to lead out waste steam from the top tower of the knockout tower, which can increase the steam pressure using as the heat source of the lithium brominate refrigerator. The device comprises at least one lithium brominate refrigerator, the top tower portion of the knockout tower on the upper portion of the esterification reaction kettle is connected on a condenser of the lithium brominate refrigerator through a steam pipe, a pressure regulating valve which can increase steam pressure in the steam pipe is connected in series on the steam pipe, and a steam branch pipe is further connected in parallel on the steam pipe, at least one air heat exchanger is connected on the steam branch pipe. The device has the characteristics of simple technology, safe, reliable and convenient usage and significant energy-saving effect, reduces the energy waste, increases the recycling usage of energy, and can really play the purpose of energy-saving and emission reduction.
Description
Technical field
What the present invention relates to is a kind of polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method and isolated plant, belongs to the production of polyester technical field.
Background technology
Existing esterification system technology, employing be the technology of PTA, EG direct esterification reaction, PTA and EG direct esterification process are the methods of directly reacting generation BHET with PTA and EG, also claim the PTA method.It is the complex process that an esterification and polycondensation are carried out simultaneously, and principal reaction comprises:
Esterification:
HOOC--COOH+2HOCH
2CH
2OH-HOCH
2CH
2OOC --COOCH
2CH
2OH+2H
2O
From the esterification equation as can be known, esterification is reversible reaction, therefore for esterification is constantly moved towards the direction that helps positive reaction, in the hope of reaching higher esterification yield, must constantly water be steamed from reflection liquid, but raw material EG continues in the reactor to participate in reaction for the EG that steams can be back to, so a process tower is set above reactor also along with water steams simultaneously when steaming water.
Esterification process is except that esterification, polycondensation main reaction, also be accompanied by the generation of numerous side reactions, as the acetaldehyde formation reaction, cyclization, glycol ether formation reaction or the like, PTA and EG direct esterification process are actually one and relate to dissolving-reaction-isolating combined process, and reaction comprises reversible esterification and polycondensation and numerous such complex reaction processes of side reaction again.
Existing production of polyester line mainly is to introduce the du pont company technology, and the polyester production device of being undertaken the construction of by safe this company of the U.S. (equipment), as shown in Figure 1.In this device, esterification is carried out in vertical tubulation esterification heat exchanger 2222-H01 and esterifying kettle 2222-R01, material in the heat exchanger 2222-H01 tube side is to come round-robin by hydrostatic pressure and thermal siphon, simultaneously, it also is to carry out in tubulation that biphase mixes, HTF supplies with heat exchanger shell pass and esterifying kettle chuck respectively, EG: the PTA mol ratio is that 1: 1.8 slurry is by the nozzle 2221-S01A/B injected system on the continuous pipeline of the same esterifying kettle of the bottom that is positioned at interchanger of a cover.System prevents esterifying kettle and well heater superpressure with rupture disk, and two rupture disks are provided, and any one of two rupture disks is online by three-way change-over valve.
The temperature of esterifying kettle chuck is adjusted the flow of heating agent by HTF pressure regulator valve PV-20104, and heating medium is that gas phase is led life, and temperature is about 330 ℃.Pressure directly to the shell side of esterification well heater, the top of heat exchanger and pipe connecting heat exchanger and esterifying kettle between provides heat by DN500 gas phase heating agent house steward HTF by pressure regulator valve PV-20102 for 3.0kg/cm2, about 330 ℃ gas phase heating agent steam of temperature.Esterification temperature is controlled at about 285 ℃.In this device, esterification is a synthesis under normal pressure.The product that produces from esterification is called prepolymer, the polymer chain that it is made up of six polymerized units, nearly 80 repeating units on the polymer chain in final polymerization reaction kettle.After the laboratory was measured the end carboxyl of carboxylate, carboxylate end carboxyl was generally about 700 at present.
The knockout tower 2223-T01 on reaction kettle of the esterification top, knockout tower working pressure are normal pressure, and the working pressure of esterifying kettle is approximate normal pressure.Water generates as by product in the esterification.Carboxylate is delivered among the prepolymerization reaction still UFPP2252/3252-R01 by pump 2231-P01, the byproduct that water, excessive EG and a spot of carboxylate are accompanied by reaction is discharged by the top of esterifying kettle 2222-R01, entering the knockout tower 2223-T01 that is installed in the reactor top is further processed, in knockout tower, gaseous substance is desuperheating at first, water distills out from heat up in a steamer a little relative higher EG with lower boiling hydrocarbon polymer, and bottom product is sent among the esterification EG jar 2223-T02 of band stirring.Part EG is by reflux into tower desuperheating steam and the steam that esterifying kettle is come in sprayed of pump 2223-P02A/B, and the EG of partial esterification jar 2223-T02 sends slurry preparing tank 2213-T01 back to, is used to prepare slurry.
After overhead product condenses in a vertical water-to-water heat exchanger 2223-H01 and cools off, collect among the return tank 2223-T03, the small part phlegma will be by the pump 2223-P01 into tower that refluxes, and the emptying of return tank enters sealed can, during first the driving, should in return tank, fill with de-salted water.
Remaining overhead product overflows to organic gas from return tank 2223-T03 and carries charging stock tank, is pumped toward organic gas stripping column 2224-T01 from this overhead product, and the steam of 3.5kg/cm2.g will be used for from water gas and carry organism.After process steam gas was carried, water was sent to sewage disposal, and the cat head material of gas stripping column will be sent in the heating agent stove to be burnt
In the design of above-mentioned complete assembly, though aspect energy-conservation, consider to some extent, but the technology when being limited to design is limit, some waste heats are not accomplished the most effective utilization, wherein the most outstanding is exactly the utilization of process tower process steam, in the past to the processing of this part steam, be to send into gas stripping column after adopting interchanger through the recirculated cooling water cooling to carry out gas and propose the pre-treatment of carrying out waste water, in this process, can cause a large amount of energy loss, be example with polymerization second phase device: 1, and the steam that process tower is 13 tons/hour can not effectively utilize, 2, cooling off this steam of 13 tons/hour needs a large amount of recirculated cooling waters.3, the wastewater temperature under the cooling is approximately about 40 ℃.Carry also and to need more than this 40 ℃ of utilization of condensed water steam heating to 100 ℃ in order effectively to carry out gas, so circulation causes the significant wastage of the energy.
Summary of the invention
The objective of the invention is to overcome the deficiency of above-mentioned existence, and a kind of minimizing energy dissipation is provided,, reach the polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method and the device of effects of energy saving and emission reduction with the recycle energy.
Polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method of the present invention, this method is: at least one lithium bromide refrigerator drawn and supplied with to the cat head exhaust steam of reaction kettle of the esterification top knockout tower as thermal source, and one holding tank is set at the condensation-water drain of refrigerator, with pump this portion water is delivered in the wastewater collection jar, part is as trim the top of column water, and other overflow to gas stripping column recycles.
The present invention increases at the pipeline of drawing exhaust steam from the cat head of knockout tower pressure regulator valve, to improve the vapor pressure as the lithium bromide refrigerator thermal source.
The present invention draws at the cat head of described knockout tower on the pipeline of exhaust steam and is parallel with one road air heat exchanger, the temperature of exhaust steam when reducing not as the lithium bromide refrigerator thermal source, make it to become waste water after the cooling, combine in the wastewater collection jar with the lithium bromide refrigerator water of condensation; Set up this air heat exchanger and can guarantee the safety moved.
Polymerization esterification residual heat using device of the present invention, it comprises at least one lithium bromide refrigerator, is connected on the condenser of lithium bromide refrigerator by steam-pipe on the cat head of reaction kettle of the esterification top knockout tower.
At least also be serially connected with the pressure regulator valve that can increase vapor pressure in the steam-pipe on the described steam-pipe, and also be parallel with one road steam branch pipe on steam-pipe, this steam branch pipe is connected with at least one air heat exchanger.
Described steam-pipe uses pipe connection on the condensation-water drain behind the condenser that connects lithium bromide refrigerator in a wastewater collection jar, and described steam branch pipe is connected in the wastewater collection jar after connecting air heat exchanger too, this wastewater collection jar one tunnel connects the knockout tower cat head, and another road is connected in gas stripping column.
The present invention to be calculating polyester output every days about 1500, but about 1800 tons of economized cycle cooling water flow per hour, economized cycle pump motor power reaches 500 degree, and 399.6 ten thousand degree that can economize on electricity are every year on average saved about 227.8 ten thousand yuan of the electricity charge.On the other hand, lithium bromide refrigerator adopts the by-product esterification steam in this project, and per hour consumption is about 20 tons, and by 50 yuan of calculating of steam per ton, the recyclable steam that utilizes reaches 43200 tons, saves 2,160,000 yuan of costs.Therefore, this project reaches postpartum, can realize that economic benefit is 443.8 ten thousand yuan every year.Therefore by technique improvement of the present invention, economic and social benefit is obvious, and it is simple to have technology, easy to use, safety, reliable, and energy-saving effect is obvious, has reduced the waste of the energy, has improved energy recycling, can really reach characteristics such as energy-saving and emission-reduction purpose.
Description of drawings
Accompanying drawing 1 is the apparatus and process syndeton synoptic diagram of prior art.
Accompanying drawing 2 is apparatus and process syndeton synoptic diagram of the present invention.
Embodiment
The present invention will be described in detail below in conjunction with accompanying drawing: the present invention is a kind of improvement to prior art, it is on the basis of existing technology, increased lithium bromide refrigerator, equipment such as air heat exchanger, and connect, so equal identical with shown in the accompanying drawing 1 such as the reaction kettle of the esterification in the accompanying drawing 2 and utility appliance and knockout tower by pipe network.
The present invention has set up the polymerization esterification residual heat using device on the basis shown in the accompanying drawing 1, described polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method is: at least one lithium bromide refrigerator drawn and supplied with to the cat head exhaust steam of reaction kettle of the esterification top knockout tower as thermal source, and one holding tank is set at the condensation-water drain of refrigerator, with pump this portion water is delivered in the wastewater collection jar, part is as trim the top of column water, and other overflow to gas stripping column is made Wastewater Pretreatment.
The present invention increases at the pipeline of drawing exhaust steam from the cat head of knockout tower pressure regulator valve, to improve the vapor pressure as the lithium bromide refrigerator thermal source.The present invention draws at the cat head of described knockout tower on the pipeline of exhaust steam and is parallel with one road air heat exchanger, the temperature of exhaust steam when reducing not as the lithium bromide refrigerator thermal source, make it to become waste water after the cooling, combine in the wastewater collection jar with the lithium bromide refrigerator water of condensation; Set up this air heat exchanger and can guarantee the safety moved.
Include polymerization esterification residual heat using device of the present invention shown in the accompanying drawing 2, it is on reaction kettle of the esterification shown in the accompanying drawing 1 and utility appliance basis thereof, also including at least one lithium bromide refrigerator, is the parallel connection combination of two lithium bromide refrigerators shown in the accompanying drawing 2.Be connected on the condenser of lithium bromide refrigerator by steam-pipe on the cat head of described reaction kettle of the esterification top knockout tower.For refrigerating efficiency and the refrigeration economy that improves lithium bromide refrigerator, need to improve the interior vapor pressure of steam-pipe as thermal source, at least also be serially connected with the pressure regulator valve that can increase vapor pressure in the steam-pipe on the described steam-pipe, and on steam-pipe, also being parallel with one road steam branch pipe, this steam branch pipe is connected with at least one air heat exchanger.The connection of this air heat exchanger can improve the security of operation.
Described steam-pipe uses pipe connection on the condensation-water drain behind the condenser that connects lithium bromide refrigerator in a wastewater collection jar, and described steam branch pipe is connected in the wastewater collection jar after connecting air heat exchanger too, this wastewater collection jar one tunnel connects the knockout tower cat head, and another road is connected in gas stripping column.Explanatory notes such as equipment in accompanying drawing 1 and the accompanying drawing 2 and utility appliance label are as the content of this specification sheets.
From the prior art analysis shown in the accompanying drawing 1 as can be known, recovery process steam of the present invention exists possibility, specifically: as can be known from the industrial analysis of prior art, in esterification, the main negative product in the normal reaction is a water, because of reaction is being carried out more than 280 ℃, so this portion water is discharged system by vapor form through process tower, simultaneously, in the esterification, need excessive EG complete with the speed that guarantees reaction and conversion.But the PTA of esterification and EG react at 1: 1, under normal pressure.The boiling point of EG is 197 ℃, therefore the EG of redundance will steam system with the water that reaction generates, the by product of this portion water and EG and other reaction generation all will be with the process tower on the esterifying kettle through after separating, EG gets back to system, water and other low by product that boils are discharged system by cat head, after the cooling of water coolant tubular heat exchange, waste water is sent to gas stripping column and handles.
According to the PFD that safe this company provided, material balance figure is as follows from each overhead product component that cat head is gone out as can be known:
Other organism of component water EG
Content (w/w) % 97.71 0.11 2.18
And in other organism, main component content is as follows:
VOC component ratio (%, volume) LEL
Acetaldehyde 65-70 4.0
The 2-methyl isophthalic acid, 3-dioxolane 25-30 2.2
1,4-diox＜5 2.0
Simultaneously according to material balance figure (PFD) that safe this company provided as can be known, under the output of 900 tons/day of normal design, the amount of the overhead product of technology cat head is 13680kg/h.Pressure is 0.05kg/cm3.
Be the better utilised existing resources simultaneously, give full play to the potentiality of existing apparatus, the Rong Sheng petrochemical industry will undergo technological transformation to conventional device, eliminate under the prerequisite of original bottleneck, and output is increased to 100 tons/day.After the transformation, the flow that process tower slips out thing is 14750kg/h, and the flow of steam will be more, and the value of utilization is also high more.
After each lithium bromide refrigerator producer is seeked advice from, learn that at present refrigerator producer is very ripe to the technology of low-pressure steam refrigerator, technically there is no too big problem, for the thermal source steam that this device provides, existing problem mainly contains following 2 points:
A. vapor pressure is low excessively, and under this pressure, the efficient of refrigerator and volume are all more uneconomical.
B. it is more that component steam contains other organism, and be slightly acidic, and general material is had corrosion, the problem that exists phlegma to reclaim simultaneously.
More than two ways to solve the problem as follows
A. improve vapor pressure
Improve vapor pressure and can adopt the form of pressure boost variable valve on the overhead vapours pipeline to pressurize, but, also need consider whether can exert an influence after the pressurization reaction because of pressurization afterreaction still pressure also increases.
In esterification process, the effect of pressure is exactly in fact to guarantee the concentration of EG in liquid phase, reduces the EG evaporation, makes the esterification system that enough hydroxyl concentrations be arranged, and successfully finishes esterification.
In esterifying kettle, because PTA and EG slurry are warmed up to 285 ℃ high temperature suddenly by normal temperature, for preventing a large amount of flash distillations of EG, pressure-controlling need be got higher, simultaneously, in the esterification, because PTA only can be partially dissolved in EG, so the initial reaction stage material is pulpous state, be heterogeneous and the simultaneous system of homogeneous phase.To homogeneous reaction, its speed of response (u) is:
u＝K·Ca(PTA)·Cb(EG)
In the formula, K is a reaction velocity constant, and a, b are respectively the reaction order of PTA, EG.
In initial reaction stage, PTA fails all to be dissolved in EG, so esterification speed is only relevant with temperature of reaction, pressure.The effect of temperature is except that changing reaction constant (K), and main is to improve the solubleness of PTA in the reaction mass liquid phase, accelerates the reaction in homogeneous phase.After PTA all dissolved, reaction mass became single liquid phase, reaches " articulation point ".Esterification speed is relevant with EG concentration with PTA again, and the concentration of EG depends on reaction pressure, and the pressure height is an EG concentration height, so speed of response is fast.But hypertonia can hinder esterification by product evaporation of water again even cause hydrolysis reaction to take place.According to above analysis as can be known, suitable raising reaction pressure to the raising of esterification speed, improves esterification yield, can provide effective steam for refrigerator, also helps esterification simultaneously, reaches the effect of killing two birds with one stone.
B. refrigerator is selected corrosion resistant material for use
For preventing the corrosion of gas phase steam to refrigerator, can select for use corrosion resistant material to make, according to use experience for many years, select for use the thin-wall stainless steel material of SS316L can effectively avoid etching problem, guarantee the long-period stable operation of equipment.
The present invention utilizes the thermal source of cat head exhaust steam as lithium bromide refrigerator, for guaranteeing enough efficient and cost of investment, needs to improve vapor pressure, for this reason,
A. on the original steam pipeline, need the pressure boost variable valve, exhaust steam pressure is improved and stablizes to 0.5kg/cm3.
B. original vapour line is DN600 (24 inches).Before newly-increased pressure regulator valve, involve DN450 (18 inches) pipeline and advance refrigerator.
C. former shell and tube recirculated water interchanger can be cancelled after transformation, when for guaranteeing operating safety, can increase an air heat exchanger newly.
The present invention selects lithium bromide refrigerator for use, a. after afterheat steam enters refrigerator, the waste water that is produced need be handled, for this reason, can one holding tank be set at the refrigerator condensation-water drain, with pump this portion water is sent among the raw wastewater holding tank 2223-T03, part is as trim the top of column water, and other overflow to gas stripping column is made Wastewater Pretreatment.
B. also have part not coagulate organic gas in the exhaust steam of Li Yonging, the degassing pipeline that the high point of refrigerator need be provided with is introduced and send into the gas stripping column recovery in the former off gas scrubber behind spray.
C. be to cooperate with former pipe network, cooling plant adopts open cycle, and the chilled water pump of this refrigerator is located at former cooling plant.The used recirculated water of refrigerator is introduced by former recirculated cooling water house steward.
Claims (6)
1, a kind of polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method, this method is: at least one lithium bromide refrigerator drawn and supplied with to the cat head exhaust steam of reaction kettle of the esterification top knockout tower as thermal source, and one holding tank is set at the condensation-water drain of refrigerator, with pump this portion water is delivered in the wastewater collection jar, part is as trim the top of column water, and other overflow to gas stripping column recycles.
2, polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method according to claim 1 is characterized in that the pipeline increase of drawing exhaust steam from the cat head of knockout tower has pressure regulator valve, to improve the vapor pressure as the lithium bromide refrigerator thermal source.
3, polymerization esterification UTILIZATION OF VESIDUAL HEAT IN method according to claim 2, the cat head that it is characterized in that described knockout tower is drawn on the pipeline of exhaust steam and is parallel with one road air heat exchanger, the temperature of exhaust steam when reducing not as the lithium bromide refrigerator thermal source, make it to become waste water after the cooling, combine in the wastewater collection jar with the lithium bromide refrigerator water of condensation.
4, a kind of polymerization esterification residual heat using device, it comprises reaction kettle of the esterification and utility appliance, it is characterized in that it also includes at least one lithium bromide refrigerator, be connected on the condenser of lithium bromide refrigerator by steam-pipe on the cat head of reaction kettle of the esterification top knockout tower.
5, polymerization esterification residual heat using device according to claim 4, it is characterized in that at least also being serially connected with on the described steam-pipe pressure regulator valve that can increase vapor pressure in the steam-pipe, and on steam-pipe, also being parallel with one road steam branch pipe, this steam branch pipe is connected with at least one air heat exchanger.
6, according to claim 4 or 5 described polymerization esterification residual heat using device, it is characterized in that on the condensation-water drain of described steam-pipe after connecting the condenser of lithium bromide refrigerator with pipe connection in a wastewater collection jar, and described steam branch pipe is connected in the wastewater collection jar after connecting air heat exchanger too, this wastewater collection jar one tunnel connects the knockout tower cat head, and another road is connected in gas stripping column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100612784A CN101250257A (en) | 2008-03-28 | 2008-03-28 | Polymerization esterification residual heat utilization method and apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100612784A CN101250257A (en) | 2008-03-28 | 2008-03-28 | Polymerization esterification residual heat utilization method and apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101250257A true CN101250257A (en) | 2008-08-27 |
Family
ID=39953873
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2008100612784A Pending CN101250257A (en) | 2008-03-28 | 2008-03-28 | Polymerization esterification residual heat utilization method and apparatus |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101250257A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102004074A (en) * | 2010-10-27 | 2011-04-06 | 中国石油化工股份有限公司 | High-temperature high-pressure gas-liquid two-phase corrosion simulated experiment device and experimental method thereof |
| WO2014144386A1 (en) * | 2013-03-15 | 2014-09-18 | Invista Technologies S.A.R.L. | Thermosiphon esterifier steam reuse |
| CN104231252A (en) * | 2014-09-01 | 2014-12-24 | 桐昆集团股份有限公司 | Polyester waste heat utilization device |
| CN110078904A (en) * | 2019-05-23 | 2019-08-02 | 上海聚友化工有限公司 | A kind of polyester esterification steam waste heat utilizes method and device |
-
2008
- 2008-03-28 CN CNA2008100612784A patent/CN101250257A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102004074A (en) * | 2010-10-27 | 2011-04-06 | 中国石油化工股份有限公司 | High-temperature high-pressure gas-liquid two-phase corrosion simulated experiment device and experimental method thereof |
| CN102004074B (en) * | 2010-10-27 | 2014-07-23 | 中国石油化工股份有限公司 | High-temperature high-pressure gas-liquid two-phase corrosion simulated experiment device and experimental method thereof |
| WO2014144386A1 (en) * | 2013-03-15 | 2014-09-18 | Invista Technologies S.A.R.L. | Thermosiphon esterifier steam reuse |
| CN105209409B (en) * | 2013-03-15 | 2017-03-08 | 因温斯特技术公司 | Thermal siphon esterification device steam recycles |
| CN104231252A (en) * | 2014-09-01 | 2014-12-24 | 桐昆集团股份有限公司 | Polyester waste heat utilization device |
| CN110078904A (en) * | 2019-05-23 | 2019-08-02 | 上海聚友化工有限公司 | A kind of polyester esterification steam waste heat utilizes method and device |
| CN110078904B (en) * | 2019-05-23 | 2023-11-07 | 上海聚友化工有限公司 | Polyester esterification steam waste heat utilization method and device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102643195B (en) | Production method of n-butyl acetate | |
| CN103044257B (en) | Terylene waste material produces alcoholysis method and the apparatus system of dioctyl terephthalate | |
| CN105112100A (en) | Continuous production technique of chlorinated paraffin | |
| CN105315132A (en) | System and method used for energy utilization between ethylene glycol device dehydrating tower and refining tower | |
| CN101250257A (en) | Polymerization esterification residual heat utilization method and apparatus | |
| CN203108242U (en) | Double-effect evaporation system used for ammonium sulphate concentration | |
| CN212102640U (en) | System for preparing acetic anhydride by acetic acid cracking-ketene method | |
| CN104844414A (en) | Equipment and process for recovering glyphosate solvent during production with glycine method | |
| CN105111052A (en) | Method for purifying acetone from waste residue and waste water produced in ketene dimmer production process | |
| CN108083984A (en) | For glyphosate solvent and the method for by-product recovery | |
| CN107460265A (en) | Blast furnace slag quenching water steam heat recovery Application way and system | |
| CN208182895U (en) | A kind of tetrahydrofuran fractional order reaction separator | |
| CN202829608U (en) | Urea deep-hydrolyzation gaseous-phase heat recovery system | |
| CN202688237U (en) | Production device for n-butyl acetate | |
| CN207143010U (en) | The dehydration device of esterification products under a kind of acid condition | |
| CN102839056B (en) | Stepped recovery and purification method and device of biodiesel methanol | |
| CN106000009B (en) | A kind of double-tower type MEDA handles landfill gas system | |
| CN205227896U (en) | Condensate water is recovery system again | |
| CN209828309U (en) | Tetrahydrofuran low-emission recovery system | |
| CN109019725A (en) | A kind of energy conservation water vaporization tower | |
| CN113413858A (en) | High molecular polymer intermediate production device and process flow | |
| CN109824481B (en) | Improvement method for improving yield of acetaldehyde system | |
| CN209696301U (en) | Adipic acid plant dust technology concentration systems | |
| CN202892954U (en) | Dual-effect distilling apparatus for concentrating mother liquid containing nitric acid | |
| CN105669380A (en) | Ethylene glycol recovery device of polyester wastewater recovery system and ethylene glycol recovery method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Open date: 20080827 |