CN100363097C - Cyclic heating system and method for chemical process - Google Patents
Cyclic heating system and method for chemical process Download PDFInfo
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- CN100363097C CN100363097C CNB2004100803355A CN200410080335A CN100363097C CN 100363097 C CN100363097 C CN 100363097C CN B2004100803355 A CNB2004100803355 A CN B2004100803355A CN 200410080335 A CN200410080335 A CN 200410080335A CN 100363097 C CN100363097 C CN 100363097C
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Abstract
The present invention relates to a cyclic heating system and a method for a chemical process. The system comprises a heating device used for heating an organic heat carrier as a heat medium, and flash evaporating kettles used for converting the liquid-phase heat medium into partial heat medium steam and heat medium condensate liquid. The present invention is characterized in that the flash evaporating kettles are arranged in a device region of a chemical production process; a plurality of high-efficiency flash evaporating kettles with different operation pressure generate the heat medium steam to heat devices and pipelines at high temperature in the device region; the heat medium condensate liquid after flash evaporation by the flash evaporating kettles is used as a heat source of a secondary heat medium cycle system for heating devices and pipelines at low temperature in the device region. The method enlarges the grading utilization of heat energy and increases the utilization efficiency of the heat energy. According to different process states of workshop production, the system is divided into the operation of a main system and a subsystem to make further energy saving of a polyester device become true.
Description
Technical field
The present invention relates to a kind of chemical process loop heating system and method.Particularly relate to and a kind ofly adopt coal furnace heating organic carrier and flash distillation to produce steam to go condensate liquid after firing equipment and the flash distillation also to can be used for the system and method for equipment and pipeline heating.This system and method can be used for the heat supply of complication system and reach precise dose control.
Background technology
In chemical production field, particularly at petrochemical industry, in the manufacture process such as polymer, because the reaction temperature height often adopts organic heat carrier to come to provide required heat energy for the reaction unit of production process as the loop heating system of heating agent.
At the mixture that adopts biphenyl and biphenyl ether is that general adopted system and method has such two characteristics in the prior art of loop heating system of heating agent:
The one, heating agent flash distillation still and heating furnace are arranged in the stove district as a whole in the prior art.In the stove district, after heating agent becomes the heating agent steam through heating furnace heating back, by the flash distillation still, be sent to the process units district far away again from the stove district.At last, the low temperature heating agent condensate liquid in process units district also melts down district's heating with pumping again.So move in circles.
The 2nd, be used for heating that the equipment of heating agent adopts mostly is to be the fuel oil heating of the energy with fuel oil.Particularly in the heating agent flash distillation generation heating agent steam of heating system make to(for) lower boiling organic matter, what then all adopt is to heat heating agent with oil burning boiler.
This loop heating system of prior art because flash evaporation unit is arranged in the stove district and away from the process units district, therefore no matter for the stove district still for the process units district, all exist flow process complexity, table of equipment number many, and be unfavorable for energy-conservation shortcoming.
Why prior art adopts with fuel oil is the fuel oil heating of the energy, and does not adopt coal-fired furnace, mainly is because for coal-fired furnace, and the organic heat carrier outlet temperature is difficult for accurately control.To such an extent as to make that the outlet temperature fluctuation is bigger.Because these defectives of prior art, although gas phase heating agent system advantage is a lot, it uses and but has been subjected to very big restriction, and particularly encouraging with the coal at the most of areas of China is the national conditions of fuel, especially like this.
Summary of the invention
Purpose of the present invention be exactly for overcome prior art flow process complexity, the table of equipment number is many, and be unfavorable for energy-conservation shortcoming, adopt coal furnace heating liquid phase organic heat carrier, flash distillation produces the closed system that gas phase heating agent and condensate liquid utilize step by step and reaches energy-conservation, simplifies flow process and accurately control the purpose of heating process on the spot.
One of the present invention's chemical process loop heating system is achieved in that
A kind of loop heating system of chemical process, described system comprises the heater that is used to heat as the organic heat carrier of liquid phase heating agent, flash distillation still, condensate liquid collection recovery and the liquid phase heating agent circulatory system that is used for described liquid phase heating agent is converted into part gas phase heating agent, it is characterized in that:
Described flash distillation still is arranged in the device zone of chemical process; The heating agent that the different efficient flash distillation still of several operating pressures produces offers the reactor device district in as the heating heating agent, and the high-temperature liquid-phase heating agent that stays after the while flash distillation offers the liquid phase heating agent circulatory system as thermal source.
Loop heating system of the present invention, used heater is preferentially selected coal furnace.
Loop heating system of the present invention, specifically can be by the use thermic load and the distribution situation that are heated equipment or pipeline in the device zone, determine quantity, layout and the physical dimension of flash distillation still, and it is arranged near the bigger reactor of the consumption heat energy in device zone.
Loop heating system of the present invention specifically can be to be used for the reaction heating system of described heating system for reaction heating-up temperature chemical process between 240～360 ℃, and the used organic carrier of described heating system is the mixture of biphenyl and biphenyl ether.
Loop heating system of the present invention specifically can be that being used for terephthalic acid (TPA) and dihydroxylic alcohols is the loop heating system that raw material is produced the continuous polymerization unit of polyphenyl dioctyl phthalate and glycol ester.
Described coal furnace district arranged apart of loop heating system of the present invention and process units zone standoff distance are 20～500m, preferred 30m.
The used organic carrier of loop heating system of the present invention can be the mixture of biphenyl and biphenyl ether, and the heating-up temperature scope is at 240～360 ℃, preferred 300～360 ℃.
The method of the present invention's two chemical process loop heating system is achieved in that
The method of operating of loop heating system of the present invention, the operating condition of described system adopts collecting and distributing control system to control according to the device technique situation, promptly be heated equipment and pipeline in the coal-fired furnace that is arranged in the stove district and the flash distillation still, heat medium circulation pump and the device zone that are arranged in the device zone, adopt pipeline and corresponding pipe fitting to link together, form an airtight system.
In concrete the enforcement, above-mentioned system can for system for being the loop heating system of the continuous polymerization unit of the production polyphenyl dioctyl phthalate of raw material and glycol ester with terephthalic acid (TPA) and dihydroxylic alcohols, in described device zone, be arranged as the flash distillation still that esterification, polycondensation provide two or more generation heating agent steam of reaction needed heat energy; Simultaneously, arrange that several utilize the condensate liquid after the flash distillation to be the secondary heating agent circulatory system of thermal source.
Production process of the present invention, be that lower (0.01～0.35Mpa) the organic matter biphenyl and the mixture of biphenyl ether are as heating agent, on this heating agent prior art basis simple in structure to heated equipment heat transfer efficiency height and reactor jacket using operating pressure, with traditional, carry out flash distillation at Lu Qu, produce the changing and simplifies of flow process of heating agent steam, and the characteristics realization of the conjugated polymer technological process of producing.
Implementation process of the present invention is described below (with reference to the accompanying drawing 1 of back):
Primary fluid system of the present invention (being major circulatory system), can be by main circulation pump P1, circulating pump P3, heating agent heating furnace H1/H2, several heating agent flash distillation still that is arranged in the process units district, such as T1 (esterification flash distillation still), T2 compositions such as (polycondensation flash distillation stills), this system is that heating furnace provides heat, Partial Liquid Phase heating agent flash distillation simultaneously to produce the system of gas phase heating agent process to liquid phase heating agent system.
Above-mentioned gas phase heating agent process comprises the generation of gas phase heating agent, heating process and removal process, can be made up of the primary fluid subsystem of several different instructions for uses.Each primary fluid subsystem all comprises flash distillation still T1/T2, is heated equipment or pipeline E1/E2, condensate liquid recycling can T3/T4 and reclaims pump P2/P5 etc.When the temperature of the liquid phase of primary fluid system is higher than in the still liquid phase heating agent boiling temperature and pressure greater than gassy system, just has the heating agent flash process among the flash distillation still T1/T2 and occur.Under identical flow condition, the temperature difference that the temperature that the liquid phase heating agent enters flash vessel is higher than liquid phase heating agent boiling point in the still is big more, and the gas phase heating agent amount that flash distillation produces is also many more.The gas phase heating agent is emitted heat and condensation in being heated equipment or pipeline, gas phase heating agent condensate liquid flow back among the recycling can T3/T4 under the effect of gravity, and then send back to and return heating furnace after heating agent condensate liquid after main circulation pump P1 inlet and the flash distillation converges by reclaiming pump P2/P5, use moves in circles after being heated.
The secondary heating agent circulatory system of the present invention (being liquid phase heating agent heating system), can by comprise the high temperature heating agent E7 of system, in equipment such as the warm matchmaker E8 of system and low temperature heating agent E9 of system constitute;
Above-mentioned liquid phase heating agent heating system, can divide several different instructions for uses, secondary heating agent cycle subsystem independently.Wherein, each system is by circulating pump P6/P7/P8 and heated equipment or pipeline E7/E8/E9 formation.The heating agent condensate liquid of the thermal source of system after from the flash distillation of flash distillation still T1 or flash distillation still T2.Heating agent condensate liquid after the flash distillation is injected in this system by circulating pump, and the equivalent low temperature heating agent condensate liquid after the heat exchange is discharged among the heating agent recycling can T4.And then send back to and return heating furnace after heating agent condensate liquid after main circulation pump P1 inlet and the flash distillation converges by reclaiming pump P5, use moves in circles after being heated.
In sum, loop heating system of the present invention and method, because the classification utilization that has strengthened heat energy, improved the utilization ratio of heat energy, and it is different according to the state of the art (system's cold conditions running, the hot running of system, esterification system start-stop car, polycondensation system start-stop car and total system start-stop car) of Workshop Production, it is primary fluid system and subsystem that system is divided into main system, and the operation of secondary heating agent system and subsystem.System and method of the present invention makes further energy-conservation the becoming a reality of polyester device.
Because the system structure characteristic and the method for operating of the above-mentioned uniqueness of the present invention, the present invention compared with prior art has following outstanding advantage:
1. the present invention has been owing to adopted the compound mode of heating agent flash distillation still and gaseous pressure regulating system, overcome coal furnace heating liquid phase organic heat carrier and made the bigger defective of outlet temperature fluctuation, temperature control precision＜± 1.0 of device internal reaction device ℃.
2. polyester device energy-saving effect of the present invention is 75% of a similar imported unit.
3. because flash distillation still of the present invention is arranged in the device zone of chemical process, effectively utilized the accumulation of energy effect of circulation liquid phase heating agent, overcome prior art and carried the gas phase heating agent to need overheated shortcoming.Therefore, heating agent heater outlet temperature of the present invention is compared with similar imported unit can reduce by 20～35 ℃, and operating temperature＜328 ℃ are also very helpful for the long-term use of the mixture of biphenyl and biphenyl ether simultaneously.
4. because heating agent flash distillation still of the present invention and circulating pump have been arranged in the device zone, and appliance arrangement heats up can be from low temperature, the heating rate of easier control appliance has overcome the defective that former flow process heats up and cooling is too fast, has protected the security of device.
5. because heating agent flash distillation still of the present invention and circulating pump have been arranged in the device zone, thereby reduced the dangerous grade in stove district, simplified the apparatus arrangement of stove district, particularly burning coal boiler room greatly.
6. because heating agent flash distillation still of the present invention and circulating pump have been arranged in the device zone, can separate the operation of heating furnace these two technological operations of different nature of operation, be convenient to production management with the flash distillation still.
Description of drawings
Fig. 1 is a chemical process loop heating system schematic diagram of the present invention
Symbol description among the figure:
E1, E2-high temperature firing equipment;
E3, E4, E5, warm firing equipment among the E6-;
E7, E8, E9-low-temperature heat equipment;
H1, the H2-coal-fired furnace;
The P1-main circulation pump;
P2, P5-reclaims pump;
P3, P4-circulating pump;
P6, P7, P8-internal circulation pump;
T1, T2-flash distillation still;
T3, T4-reclaims still.
The specific embodiment
Below, in conjunction with shown in Figure 1, with produce per year 80,000 tons be that raw material is produced the polyphenyl dioctyl phthalate and the glycol ester continuous polymerization unit is a specific embodiment with terephthalic acid (TPA) and ethylene glycol, to being described in detail as follows of chemical process loop heating system of the present invention:
The coal-fired heating agent heating furnace H1/H2 of native system, its heat medium outlet temperature is 310～330 ℃, pressure is＜0.6Mpa.Liquid phase heating agent after the heating furnace heating is delivered in the polyester device esterification and two heating agent flash vessels of polycondensation T1/T2 on the spot.Gas phase heating agent after the flash distillation offers reactor in the device as the heating heating agent, and the high-temperature liquid-phase heating agent that flash distillation simultaneously stays is made thermal source, offers the secondary heating agent circulatory system (being the liquid phase heating agent circulatory system) and uses (heating or cooling).
1) needs adopt the equipment and the pipeline of vapour phase heating agent, by heating agent flash distillation still, obtain the gas phase heating agent with the flash distillation in heating agent flash vessel (T1) of overheated liquid phase heating agent, the serviceability temperature scope of gas phase heating agent is 300～320 ℃, and pressure limit is between 0.14～0.24MPa;
2) need adopting the equipment and the pipeline of liquid phase heating agent, is 290～310 ℃ liquid phase heating agent with the part heating agent condensate temperature after the polycondensation heating agent flash vessel T2 flash distillation, is infeeded the secondary heating agent circulatory system that is formed by heat medium circulation pump separately by pump.Control 260～280 ℃ of the serviceability temperatures of each secondary heating agent circulatory system by the inlet adjusting valve, the circulation of secondary heating agent is played the bigger heating agent internal circulating load of assurance, is reduced the effect of heating agent serviceability temperature difference, and the heating, insulation that make equipment are evenly.
Be described in further detail, system of the present invention can be broken down as follows:
1. the primary fluid circulatory system (being the gas phase heating agent circulatory system)
Its heat supplying process is: by main circulation pump P1, be arranged in the heating agent heating furnace H1/H2 in stove district and the flash distillation of heating agent on the spot still T1, T2 that two are arranged in the process units district form, be by heating furnace heat energy to be offered heating agent, heating agent offers heat energy the system of equipment such as reactor again.
The heating process of its gas phase heating agent is: the liquid phase heating agent of primary fluid progressively heats up and when reaching boiling temperature, just there is the heating agent flash process to occur among flash vessel T1, the T2, the temperature difference that the temperature that major cycle liquid phase heating agent enters flash vessel is higher than liquid phase heating agent boiling point in the still is big more, and the gas phase heating agent amount of flash distillation is also many more.
(1) user of the gas phase heating agent of esterification heating agent flash distillation still T1 generation is the esterifier system, comprising: esterification heater E1 and esterifying kettle E2, and the heating agent lime set after the use is directly returned the outlet at bottom of heating agent flash distillation still T1, imports primary fluid circulating pump P1;
(2) user of the gas phase heating agent of polycondensation heating agent flash distillation still T2 generation is the polycondensation reactor system, comprise: the E6 of upper gaseous phase system of precondensation heater E3, precondensation still E4 and discharge nozzle, whole polycondensation vessel E5 and two polycondensation reactors, the heating agent lime set after these 4 parts are used is accepted by recycling can T4.
(3) the collected heating agent lime set of part heating agent condensate liquid after the flash distillation and pans T4 is sent back to the outlet at bottom of esterification heating agent flash vessel T1 respectively among the polycondensation heating agent flash distillation still T2 by heating agent pump P3 and P5, imports the primary fluid major circulatory system.
2. the secondary heating agent circulatory system (being the liquid phase heating agent circulatory system)
Liquid phase heating agent heating system can be divided into 3 independently secondary heating agent circulatory systems:
(1) secondary heating agent circulatory system E7 is for the positions such as top cover of esterifying kettle top coil pipe, bottom U type pipe and polycondensation spray condenser provide heat tracing;
(2) secondary heating agent circulatory system E8 for still, ethylene glycol steam jet pump at the bottom of oligomer pipette line, the esterification knockout tower provide heat, also provides the cooling heating agent and provides the evaporation thermal source for the ethylene glycol evaporimeter for melt cooler;
(3) secondary heating agent circulatory system E9 is for terminal polymerization kettle exports to granulation and the Direct Spinning melt pipe provides the insulation heat.
The part heating agent condensate liquid of the heat supplement of the liquid phase heating agent circulatory system after by flash distillation among the polycondensation heating agent flash distillation still T2 provides through pump P3, low temperature heating agent after the use is got back among the heating agent pans T4, send the outlet at bottom of esterification heating agent flash distillation still T1 back to by the outlet pump P5 of heating agent pans T4, import the primary fluid major circulatory system.
Claims (9)
1. the loop heating system of a chemical process, described system comprises the heater that is used to heat liquid phase heating agent organic carrier, the circulatory system that is used for described liquid phase heating agent is converted into flash distillation still, heating agent condensate liquid collection recovery and the liquid phase heating agent of part gas phase heating agent, it is characterized in that:
Described flash distillation still is arranged in the device zone of chemical process; The heating agent that the different efficient flash distillation still of several operating pressures produces offers the reactor device district in as the heating heating agent, and the high-temperature liquid-phase heating agent that stays after the while flash distillation offers the liquid phase heating agent circulatory system as thermal source.
2. loop heating system as claimed in claim 1 is characterized in that: the used heater of described system is a coal furnace.
3. loop heating system as claimed in claim 2, it is characterized in that: described heating system is the reaction heating system of reaction heating-up temperature chemical process between 240～360 ℃, and the used organic carrier of described heating system is the mixture of biphenyl and biphenyl ether.
4. loop heating system as claimed in claim 3 is characterized in that: described heating system is for terephthalic acid (TPA) and dihydroxylic alcohols being the loop heating system of the continuous polymerization unit of raw material production polyphenyl dioctyl phthalate and glycol ester.
5. loop heating system as claimed in claim 3 is characterized in that: described coal furnace district and process units zone standoff distance are 20～500m.
6. loop heating system as claimed in claim 5 is characterized in that: described coal furnace district and process units zone standoff distance are 30m.
7. loop heating system as claimed in claim 3 is characterized in that: described heating furnace heating-up temperature is between 300～360 ℃.
8. as the method for operating of the described loop heating system of one of claim 1～7, it is characterized in that: the operating condition of described system adopts collecting and distributing control system to control according to the device technique situation, promptly to heated equipment and pipeline in the coal-fired furnace that is arranged in the stove district and the flash distillation still, heat medium circulation pump and the device zone that are arranged in the device zone, adopt pipeline and corresponding pipe fitting to link together, form an airtight system.
9. method of operating as claimed in claim 8, it is characterized in that: described system is for being the loop heating system of the continuous polymerization unit of the production polyphenyl dioctyl phthalate of raw material and glycol ester with terephthalic acid (TPA) and dihydroxylic alcohols, is arranged as the flash distillation still that esterification, polycondensation provide two or more generation heating agent steam of reaction needed heat energy in described device zone; Simultaneously, arrange that several utilize the condensate liquid after the flash distillation to be the secondary heating agent circulatory system of thermal source.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100803355A CN100363097C (en) | 2004-09-29 | 2004-09-29 | Cyclic heating system and method for chemical process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100803355A CN100363097C (en) | 2004-09-29 | 2004-09-29 | Cyclic heating system and method for chemical process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1754621A CN1754621A (en) | 2006-04-05 |
| CN100363097C true CN100363097C (en) | 2008-01-23 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100803355A Expired - Fee Related CN100363097C (en) | 2004-09-29 | 2004-09-29 | Cyclic heating system and method for chemical process |
Country Status (1)
| Country | Link |
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| CN (1) | CN100363097C (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01315336A (en) * | 1988-06-15 | 1989-12-20 | Tlv Co Ltd | Heating and cooling device for reactor |
| CN1252865A (en) * | 1997-03-05 | 2000-05-10 | 科夫克斯公司 | Method and apparatus for heat transfer |
| CN1528507A (en) * | 2000-01-14 | 2004-09-15 | Tlv | Steam heating device |
-
2004
- 2004-09-29 CN CNB2004100803355A patent/CN100363097C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01315336A (en) * | 1988-06-15 | 1989-12-20 | Tlv Co Ltd | Heating and cooling device for reactor |
| CN1252865A (en) * | 1997-03-05 | 2000-05-10 | 科夫克斯公司 | Method and apparatus for heat transfer |
| CN1528507A (en) * | 2000-01-14 | 2004-09-15 | Tlv | Steam heating device |
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| Publication number | Publication date |
|---|---|
| CN1754621A (en) | 2006-04-05 |
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