CN205391776U - Chemical plant installations - Google Patents
Chemical plant installations Download PDFInfo
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- CN205391776U CN205391776U CN201620160199.9U CN201620160199U CN205391776U CN 205391776 U CN205391776 U CN 205391776U CN 201620160199 U CN201620160199 U CN 201620160199U CN 205391776 U CN205391776 U CN 205391776U
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Abstract
The utility model discloses a chemical plant installations, including MTBE device and aromatic hydrocarbon device, the MTBE device includes a plurality of rectifying columns, the reboiler series connection of a plurality of rectifying columns, and the aromatic hydrocarbon device includes the cryogenic heat exchanger series connection of a plurality of fractionating towers, a plurality of fractionating towers, cryogenic heat exchanger's heat medium medium export is connected with the heat medium medium inlet of reboiler, and the heat medium medium export of reboiler is connected with cryogenic heat exchanger's heat medium medium inlet. The utility model provides a pair of chemical plant installations adopts the mode of ladder intensification or cooling to carry out the heat transfer, need not can practice thrift the corresponding energy heating or cool off the heat medium medium use amount of circulation medium when just having avoided heating or cooling. Heat transfer between aromatic hydrocarbon device and MTBE device and the heat medium medium is mutually supported, and cooling, heating load are close to the samely, in certain extent, and heat source and hot trap can balance by oneself for the operating efficiency of device is higher.
Description
Technical field
This utility model relates to chemical plant installations heat recovery technology field, particularly relates to a kind of chemical plant installations.
Background technology
In petrochemical plant, aromatic device is, by modes such as rectification, aromatic hydrocarbons mixture is separated into single material, such as benzene,toluene,xylene etc.；MTBE device obtains olefin compound and methyl tertiary butyl ether(MTBE) in the same way, in separation process, because the boiling point difference of various materials is very big, so the temperature required heat to when separating is different, the temperature required major part of such as aromatic hydrocarbons is more than 120 DEG C, and MTBE device is temperature required for 55-65 DEG C, in order to reduce energy waste, saving the energy, industry proposes the method that can utilize mutually heat.
At present, conventional method be that thermal medium temperature reduces in MTBE device and thermal medium heat exchange, and afterwards, thermal medium and aromatic device heat exchange, thermal medium temperature raises, and further supplying MTBE device, so circulates.Wherein, include two rectifying columns for MTBE device respectively and aromatic device includes two fractionating columns, the reboiler of two rectifying columns is connected in parallel, wherein, temperature respectively 72 DEG C and 85 DEG C after thermal medium cooling, thermal medium is before being fed separately to fractionating column, it is cooled to 72 DEG C by thermal medium cooler, afterwards, it is re-supplied to two fractionating columns and tower overhead gas heat exchange, after heat exchange, the thermal medium of (intensification) is further heated after 95 DEG C by steam heater, it is fed separately to rectifying column again, repetitive cycling, as shown in Figure 1, this kind of endless form make use of partial heat, reduce thermal loss, also reduce and add thermogenetic energy loss.
But, in this kind of endless form, it is necessary to thermal medium cooler is set and thermal medium is lowered the temperature and heats up by steam heater respectively.Therefore, thermal medium cooler and steam heater have certain energy loss.Meanwhile, in whole blood circulation, it is impossible to realize the self-balancing of thermal medium temperature, it is necessary to the external world is adjusted, operation and maintenance workload are increased.
Utility model content
The purpose of this utility model is in that to propose a kind of chemical plant installations, to solve the consumption of increase energy consumption and the circulatory mediator existed in prior art, and needs the external world to regulate, it is impossible to realize the technical problem of self-balancing.
For reaching this purpose, this utility model by the following technical solutions:
A kind of chemical plant installations, including MTBE device and aromatic device, described MTBE device includes multiple rectifying column, and the reboiler of multiple described rectifying columns is connected in series, and described aromatic device includes multiple fractionating column, and the cryogenic heat exchanger of multiple described fractionating columns is connected in series；
The thermal medium outlet of described cryogenic heat exchanger is connected with the thermal medium entrance of described reboiler, and the thermal medium outlet of described reboiler is connected with the thermal medium entrance of described cryogenic heat exchanger.
Further, it is connected to heater between thermal medium outlet and the thermal medium entrance of described reboiler of described cryogenic heat exchanger.
Further, described MTBE device includes the first rectifying column and Second distillation column, and the reboiler of described first rectifying column and Second distillation column is connected in series；
Described aromatic device includes the first fractionating column and after-fractionating tower, and the cryogenic heat exchanger of described first fractionating column and described after-fractionating tower is connected in series.
Further, the raw material of described thermal medium is heat medium water.
Further, it is connected to heating agent water pot between thermal medium outlet and the thermal medium entrance of described cryogenic heat exchanger of described reboiler.
Further, described heater is steam heater.
A kind of chemical plant installations that this utility model provides, during use, thermal medium one by one carry out heat supply or cooling, the mode adopting series connection carries out heat exchange, concrete, in aromatic device, first pass through the cryogenic heat exchanger of first fractionating column, after heat exchange, thermal medium temperature raises, afterwards, enter back into the cryogenic heat exchanger of next fractionating column, temperature is further improved, after aromatic device completes heat exchange, thermal medium enters into MTBE device, first pass through the reboiler of first rectifying column, after heat exchange, temperature reduces, afterwards, enter back into the reboiler of next rectifying column, temperature further reduces, after MTBE device completes heat exchange, thermal medium is re-introduced in aromatic device to carry out heat exchange, so circulate.
This chemical plant installations, in aromatic device and MTBE device, adopts the mode of ladder-elevating temperature or cooling to carry out heat exchange, it is not necessary to thermal medium being heated or is cooling down, and therefore, it can save the corresponding energy, and when avoiding heating or cooling circulatory mediator make consumption.Heat exchange between aromatic device and MTBE device and thermal medium cooperates, and cooling, heating load are close to identical, and therefore, within the specific limits, thermal source and hot trap can balance voluntarily so that the operational efficiency of device is higher.
Accompanying drawing explanation
Fig. 1 is the structural schematic block diagram of prior art；
Fig. 2 is the FB(flow block) of a kind of chemical plant installations waste heat reclaiming process that this utility model embodiment provides；
Fig. 3 is the structural schematic block diagram of a kind of chemical plant installations that this utility model embodiment provides.
In figure:
1, rectifying column；2, reboiler；3, fractionating column；4, cryogenic heat exchanger；5, heater；6, heating agent water pot.
Detailed description of the invention
The technical solution of the utility model is further illustrated below in conjunction with accompanying drawing and by detailed description of the invention.
Embodiment 1
As Figure 2-3, a kind of chemical plant installations waste heat reclaiming process, comprise the following steps:
The thermal medium of circulation carries out heat exchange with the cryogenic heat exchanger 4 in multiple fractionating columns 3 of aromatic device, and multiple cryogenic heat exchangers 4 are serially connected, and the temperature of thermal medium gradually rises；
The reboiler 2 of multiple rectifying columns 1 of the thermal medium after intensification and MTBE device carries out heat exchange, and multiple reboilers 2 are serially connected, and the temperature of thermal medium is gradually lowered；
The thermal medium of cooling resupplies the fractionating column 3 of aromatic device as the thermal medium circulated, and thermal medium recycles.
In existing waste-heat recovery device, the mode adopting heat supply in parallel carries out heat exchange, wherein, in different rectifying column 1/ fractionating columns 3, the temperature of the heat medium water after heat exchange is different, therefore, before once circulating on entering, it is necessary to carry out cooling down or heating up, after reaching the temperature specified, it is circulated use again, therefore, it is necessary to arrange cooler and heater.
And in this technique, employing is stepped heat exchange mode, temperature gradually rises/reduces, and therefore, by the Temperature numerical after control heat exchange, can realize temperature control such that it is able to realize the self-balancing of temperature, it is easy to management.
Thermal medium after heating, by, after aromatic device, thermal medium being heated, is re-fed into MTBE device by thermal medium.
Preferably, can be heated before thermal medium enters into MTBE device, wherein, corresponding heater 5 not normally open, it is not heated under normal operating conditions, its object is to avoid, in self-balancing process, the situation that temperature reduces occurring.Optionally being heated for thermal medium, relatively existing device, energy consumption and circulatory mediator (steam, recirculated water etc.) use still relatively low.
Embodiment 2
As Figure 2-3, a kind of chemical plant installations, including MTBE device and aromatic device, MTBE device includes multiple rectifying column 1, and the reboiler 2 of multiple rectifying columns 1 is connected in series, and aromatic device includes multiple fractionating column 3, and the cryogenic heat exchanger 4 of multiple fractionating columns 3 is connected in series；
The thermal medium outlet of cryogenic heat exchanger 4 is connected with the thermal medium entrance of reboiler 2, and the thermal medium outlet of reboiler 2 is connected with the thermal medium entrance of cryogenic heat exchanger 4.
It is connected to heater 5 between thermal medium outlet and the thermal medium entrance of reboiler 2 of cryogenic heat exchanger 4.
The effect of heater 5 is that thermal medium is heated, and wherein, the effect of heater 5 is in good time unlatching, only plays preventive effect, and the temperature further avoided the occurrence of reduces, the problem of temperature range during beyond self-balancing.The state of long-time unlatching is not started from, so that still can save circulatory mediator makes consumption due to heater 5.Wherein, it is preferred that heater 5 is steam heater.During use, recirculated water and cyclic steam make consumption relatively low.
Preferably, the raw material of thermal medium is heat medium water.
MTBE device includes the first rectifying column and Second distillation column, and the reboiler 2 of the first rectifying column and Second distillation column is connected in series；
Aromatic device includes the first fractionating column and after-fractionating tower, and the cryogenic heat exchanger 4 of the first fractionating column and after-fractionating tower is connected in series.
Two rectifying columns 1 and two fractionating columns 3 are all included for MTBE device and aromatic device, initial state, the temperature of heat medium water is 72 DEG C, after the cryogenic heat exchanger 4 of the first fractionating column and after-fractionating tower, the temperature of heat medium water is thus lifted to 95 DEG C, afterwards, heat medium water enters into the reboiler 2 of the first rectifying column, heat medium water carries out heat supply, and temperature is reduced to 85 DEG C, afterwards, enter back into the reboiler 2 of Second distillation column, temperature is reduced to 72 DEG C, and heat medium water is re-introduced into aromatic device, so circulates.
Wherein, in use, can there is ± the error of 5 DEG C in the temperature of the heat medium water that aromatic device and MTBE device flow out, wherein, carrying out cryogenic heat exchanger 4 carrying out heat supply for cold-peace reboiler 2, temperature variation is fixing, it is possible to guarantee being smoothed out of self-balancing every time.When the bigger situation of the temperature difference occurs, by heater 5, heat medium water is heated, its temperature is promoted to 95 DEG C.
It is connected to heating agent water pot 6 between thermal medium outlet and the thermal medium entrance of cryogenic heat exchanger 4 of reboiler 2.
Wherein, heating agent water pot 6 connects water pump, by water pump, heat medium water is delivered to aromatic device, can supplement heat medium water raw material at heating agent water pot 6 place.
A kind of chemical plant installations that above-described embodiment provides, during use, thermal medium one by one carry out heat supply or cooling, the mode adopting series connection carries out heat exchange, concrete, in aromatic device, first pass through the cryogenic heat exchanger 4 of first fractionating column 3, after heat exchange, thermal medium temperature raises, afterwards, enter back into the cryogenic heat exchanger 4 of next fractionating column 3, temperature is further improved, after aromatic device completes heat exchange, thermal medium enters into MTBE device, first pass through the reboiler 2 of first rectifying column 1, after heat exchange, temperature reduces, afterwards, enter back into the reboiler 2 of next rectifying column 1, temperature further reduces, after MTBE device completes heat exchange, thermal medium is re-introduced in aromatic device to carry out heat exchange, so circulate.
This chemical plant installations waste heat reclaiming process and chemical plant installations, in aromatic device and MTBE device, the mode adopting ladder-elevating temperature or cooling carries out heat exchange, without thermal medium being heated or cooling down, therefore, can save the corresponding energy, and when avoiding heating or cooling circulatory mediator make consumption.Meanwhile, the heat exchange between aromatic device and MTBE device and thermal medium cooperates, and cooling, heating load are close to identical, and therefore, within the specific limits, thermal source and hot trap can balance voluntarily so that the operational efficiency of device is higher.
Concrete in the process of chemical residual heat recycling, two reboilers of MTBE and two cryogenic heat exchangers of aromatic device are selected to be connected in series or be connected in parallel, mainly determines according to the temperature of heat medium water and for the temperature of medium that heats.Temperature for MTBE device the first rectifying column and the reboiler of Second distillation column, when the temperature of the medium of two reboilers identical (60 DEG C), two reboilers select to be connected in parallel, heat medium water is divided into two and is respectively fed in reboiler to carry out heat exchange, finally, the heat medium water of 72 DEG C is obtained.
If the temperature of the medium of two reboilers one is 65 DEG C, one when being 55 DEG C, then two reboilers select to be connected in series, and heat medium water is first all flowed into the reboiler of 65 DEG C and carries out heat exchange, and heat medium water temperature drops to about 85 DEG C, afterwards, the reboiler being flowed into 55 DEG C again carries out heat exchange, finally obtains the heat medium water of 72 DEG C, enters back into heat exchange in aromatic device, wherein, the cryogenic heat exchanger in aromatic device is determined in the same fashion.
If the temperature of the medium of two reboilers one is 65 DEG C, one is 55 DEG C, reboiler adopts connected mode in parallel, obtain the heat medium water of 72 DEG C, if heat medium water is divided into two, it is necessary to increase reboiler, if reboiler is constant, then needing to carry more heat medium water, what adopt in above two mode any all can occur that cost improves, the situation that energy consumption improves.
Therefore, the temperature in actual chemical residual heat recovery process, according to the temperature of actual heat medium water and heat transferring medium, it is determined that the connected mode of the reboiler of MTBE device and the cryogenic heat exchanger of aromatic device.
Know-why of the present utility model is described above in association with specific embodiment.These describe and are intended merely to explanation principle of the present utility model, and can not be construed to the restriction to this utility model protection domain by any way.Based on explanation herein, those skilled in the art need not pay performing creative labour can associate other detailed description of the invention of the present utility model, and these modes fall within protection domain of the present utility model.
Claims (6)
1. a chemical plant installations, it is characterized in that, including MTBE device and aromatic device, described MTBE device includes multiple rectifying column (1), the reboiler (2) of multiple described rectifying columns (1) is connected in series, described aromatic device includes multiple fractionating column (3), and the cryogenic heat exchanger (4) of multiple described fractionating columns (3) is connected in series；
The thermal medium outlet of described cryogenic heat exchanger (4) is connected with the thermal medium entrance of described reboiler (2), and the thermal medium outlet of described reboiler (2) is connected with the thermal medium entrance of described cryogenic heat exchanger (4).
2. chemical plant installations according to claim 1, it is characterised in that be connected to heater (5) between thermal medium outlet and the thermal medium entrance of described reboiler (2) of described cryogenic heat exchanger (4).
3. chemical plant installations according to claim 1, it is characterised in that described MTBE device includes the first rectifying column and Second distillation column, the reboiler (2) of described first rectifying column and Second distillation column is connected in series；
Described aromatic device includes the first fractionating column and after-fractionating tower, and the cryogenic heat exchanger (4) of described first fractionating column and described after-fractionating tower is connected in series.
4. chemical plant installations according to claim 1, it is characterised in that the raw material of described thermal medium is heat medium water.
5. chemical plant installations according to claim 1, it is characterised in that be connected to heating agent water pot (6) between thermal medium outlet and the thermal medium entrance of described cryogenic heat exchanger (4) of described reboiler (2).
6. chemical plant installations according to claim 2, it is characterised in that described heater (5) is steam heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620160199.9U CN205391776U (en) | 2016-03-02 | 2016-03-02 | Chemical plant installations |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201620160199.9U CN205391776U (en) | 2016-03-02 | 2016-03-02 | Chemical plant installations |
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| Publication Number | Publication Date |
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| CN205391776U true CN205391776U (en) | 2016-07-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201620160199.9U Expired - Fee Related CN205391776U (en) | 2016-03-02 | 2016-03-02 | Chemical plant installations |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105617706A (en) * | 2016-03-02 | 2016-06-01 | 上海优华系统集成技术股份有限公司 | Waste heat recovery technology for chemical engineering device and chemical engineering device |
-
2016
- 2016-03-02 CN CN201620160199.9U patent/CN205391776U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105617706A (en) * | 2016-03-02 | 2016-06-01 | 上海优华系统集成技术股份有限公司 | Waste heat recovery technology for chemical engineering device and chemical engineering device |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20160727 Termination date: 20210302 |
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| CF01 | Termination of patent right due to non-payment of annual fee |