CN213955673U - Hydrogenation reactant heat recycling system - Google Patents
Hydrogenation reactant heat recycling system Download PDFInfo
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- CN213955673U CN213955673U CN202023192522.6U CN202023192522U CN213955673U CN 213955673 U CN213955673 U CN 213955673U CN 202023192522 U CN202023192522 U CN 202023192522U CN 213955673 U CN213955673 U CN 213955673U
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Abstract
The utility model relates to a hydrogenation reactant heat recycle system, including heat medium water storage tank, the cooling heat exchanger that intensification heat exchanger and at least one-level heat energy utilization of at least one-level heat energy recovery, heat medium water storage tank passes through outlet conduit and the cold medium feed inlet intercommunication of intensification heat exchanger, the hot medium feed inlet of intensification heat exchanger and hydrogenation reaction system's high temperature feed liquid pipeline intercommunication, the hot medium discharge gate of intensification heat exchanger and settling kettle's feed inlet intercommunication, the hot medium discharge gate of intensification heat exchanger passes through the hot medium feed inlet intercommunication of intermediate junction pipeline with the cooling heat exchanger, the hot medium discharge gate of cooling heat exchanger passes through the feed inlet intercommunication of recovery pipeline with heat medium water storage tank, set up water pump on outlet conduit, set up level gauge and thermometer on heat medium water storage tank respectively. The utility model discloses retrieve and utilize the heat energy among the hydrogenation reaction system, realize energy saving and consumption reduction's effect.
Description
Technical Field
The utility model belongs to the technical field of heat recovery, in particular to hydrogenation reactant heat recovery utilizes system.
Background
The sugar alcohol hydrogenation section is an intermittent reaction process, the raw material and hydrogen are subjected to hydrogenation reaction, the raw material and the hydrogen are heated by a steam coil, the temperature of the material is increased from 50 ℃ to 120 ℃, and the temperature after the reaction is about 130-140 ℃. At present, heat recovery is performed by heat exchange between a coil and purified water, and then the heat is used as water for tank washing and the like. But the heat recovery of the reaction product is limited, the reaction product is flashed in a settling tank, a large amount of dead steam is emptied at the top of the tank, and the heat is not recycled; on the other hand, the temperature of boiler desalted water is about 15-25 ℃, the boiler slag is heated to about 40 ℃ and enters a deaerator (104 ℃), the temperature of the desalted water is low, 0.8MPa of steam is consumed for reheating, in addition, the water for size mixing of the raw material is about 40 ℃, the 0.8MPa of steam is consumed for heating to about 60 ℃ during process size mixing, and a large amount of heat energy is consumed by the boiler desalted water and the deaerator.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a hydrogenation reactant heat recovery utilizes system is provided, after the heat medium water absorbed the heat energy of high temperature feed liquid in the hydrogenation reaction system through the heat exchanger that heaies up, rethread cooling heat exchanger carries out the heat transfer for the raw materials slurry mixing water and the boiler demineralized water of hydrogenation in proper order and heaies up, returns the heat medium water pitcher after the heat medium water heat transfer cooling again, and the heat energy in the hydrogenation reaction system is got up by make full use of like this, plays energy saving and consumption reduction's function.
The utility model discloses a realize like this, a hydrogenation reactant heat recovery utilizes system is provided, including heat medium water storage tank, the intensification heat exchanger of at least one-level heat recovery and the cooling heat exchanger of at least one-level heat utilization, heat medium water storage tank passes through outlet conduit and the cold medium feed inlet intercommunication of intensification heat exchanger, the hot medium feed inlet of intensification heat exchanger and hydrogenation reaction system's high temperature feed liquid pipeline intercommunication, the hot medium discharge gate of intensification heat exchanger and settling kettle's feed inlet intercommunication, the hot medium discharge gate of intensification heat exchanger passes through the hot medium feed inlet intercommunication of intermediate junction pipeline with cooling heat exchanger, the hot medium discharge gate of cooling heat exchanger passes through the feed inlet intercommunication of recovery pipeline with heat medium water storage tank, set up water pump on outlet conduit, set up level gauge and thermometer on heat medium water storage tank respectively.
Furthermore, a water replenishing pipeline is arranged on the heat medium water storage tank and communicated with the purification water pipe.
Furthermore, a two-stage heat energy utilization cooling heat exchanger is arranged in the hydrogenation reactant heat recycling system, the former stage cooling heat exchanger exchanges heat with the raw material slurry mixing water for the hydrogenation reaction and heats up, the latter stage cooling heat exchanger exchanges heat with the boiler desalted water for the hydrogenation reaction and heats up, a cooling intermediate pipeline is arranged in the two-stage cooling heat exchanger and is connected in series, one end of the cooling intermediate pipeline is communicated with a heat medium discharge port of the former stage cooling heat exchanger, and the other end of the cooling intermediate pipeline is communicated with a heat medium feed port of the latter stage cooling heat exchanger.
Furthermore, a brine thermometer is respectively arranged on pipelines of the boiler demineralized water inlet and outlet cooling heat exchanger, a slurry mixing water thermometer is respectively arranged on pipelines of the raw material slurry mixing water inlet and outlet cooling heat exchanger, and a cooling water thermometer is arranged on a cooling intermediate pipeline.
Furthermore, three-stage heat energy recovery warming heat exchangers are arranged in the hydrogenation reactant heat recycling system, the three-stage warming heat exchangers are connected in series through warming intermediate pipelines, one end of each warming intermediate pipeline is communicated with a cold medium discharge port of a previous stage warming heat exchanger, the other end of each warming intermediate pipeline is communicated with a cold medium feed port of a next stage warming heat exchanger, a hot medium feed port of each stage warming heat exchanger is respectively communicated with a high-temperature material liquid pipeline of the hydrogenation reaction system, and a hot medium discharge port of each stage warming heat exchanger is respectively communicated with feed ports of the settling kettles.
Furthermore, a material liquid thermometer is respectively arranged on a high-temperature material liquid inlet and outlet pipeline of the hydrogenation reaction system of each stage of the temperature-rising heat exchanger, and a temperature-rising water thermometer is respectively arranged on a temperature-rising middle pipeline.
Further, an intermediate thermometer is disposed on the intermediate connecting pipe.
Furthermore, an interface with the cleaning pipeline is arranged on the water outlet pipeline.
Compared with the prior art, the utility model discloses a hydrogenation reactant heat recovery utilizes system, heat medium water are drawn from the hot medium water tank, and after the pressurization, heat up with the high temperature feed liquid heat transfer of hydrogenation system in proper order, again in proper order with raw materials size mixing water and boiler demineralized water heat transfer, return the hot medium water tank after the heat transfer cooling again, form hot medium hydrologic cycle, the hot medium water still can be used as wasing water. Therefore, heat energy and water in the hydrogenation reaction system are fully utilized, and the functions of energy conservation and consumption reduction are achieved.
The utility model discloses still have following effect:
1. the average heat exchange amount is estimated to be 1340kW, which is equivalent to about 1.5t/h of steam of 0.8 MPa.
2. Purified water is used as a heating medium for recycling, and waste water discharge is reduced.
Drawings
Fig. 1 is a schematic structural diagram of a preferred embodiment of the present invention.
Detailed Description
In order to make the technical problem, technical solution and advantageous effects to be solved by the present invention more clearly understood, the following description is given in conjunction with the accompanying drawings and embodiments to illustrate the present invention in further detail. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
The utility model discloses preferred embodiment of hydrogenation reactant heat recovery utilizes system, the cooling heat exchanger that the intensification heat exchanger and the at least one-level heat utilization of heat recovery including heat medium water storage tank 1, at least one-level heat energy. After the heat medium water flows through the heating heat exchanger, the heat of the heat medium flowing through the heating heat exchanger is absorbed and then heated, and the heat energy of the heat medium water is recovered and then heated. After the heat medium water flows through the temperature-reducing heat exchanger, the heat of the heat medium water is absorbed by the cold medium flowing through the temperature-reducing heat exchanger and then is reduced, and the heat energy of the heat medium water is utilized and then is reduced.
As shown in fig. 1, the hydrogenation reactant heat recycling system comprises a three-stage temperature-rising heat exchanger and a two-stage temperature-lowering heat exchanger. The three-level heating heat exchangers are mutually connected in series through a heating intermediate pipeline 5, and the two-level cooling heat exchangers are provided with cooling intermediate pipelines 8 which are mutually connected in series. The three-level temperature rising heat exchanger comprises a front-level temperature rising heat exchanger 2, a middle-level temperature rising heat exchanger 3 and a rear-level temperature rising heat exchanger 4, and the two-level temperature reducing heat exchanger comprises a front-level temperature reducing heat exchanger 6 and a rear-level temperature reducing heat exchanger 7. The direction of arrows in the figure shows the direction of the material flow of the system, including purified water, high-temperature feed liquid, demineralized water, raw material slurrying water and the like.
One end of the warming middle pipeline 5 is communicated with a cold medium discharge port of the previous warming heat exchanger, and the other end of the warming middle pipeline is communicated with a cold medium feed port of the next warming heat exchanger. The heat medium feed inlet of each stage of temperature rising heat exchanger is respectively communicated with a high-temperature feed liquid pipeline of the hydrogenation reaction system, and the heat medium discharge outlet of each stage of temperature rising heat exchanger is respectively communicated with the feed inlets of the settling kettles.
The front-stage cooling heat exchanger 6 exchanges heat and heats the raw material slurry mixing water for the hydrogenation reaction, and the rear-stage cooling heat exchanger 7 exchanges heat and heats the boiler desalted water for the hydrogenation reaction. One end of the cooling intermediate pipeline 8 is communicated with a heat medium discharge hole of the front-stage cooling heat exchanger 6, and the other end of the cooling intermediate pipeline is communicated with a heat medium feed hole of the rear-stage cooling heat exchanger 7.
The heating medium water storage tank 1 is communicated with the cold medium feed inlet of the preceding-stage heating heat exchanger 2 through a water outlet pipeline 9, the heat medium feed inlet of each heating heat exchanger is communicated with the high-temperature material liquid pipeline of the hydrogenation reaction system, and the heat medium discharge outlet of each heating heat exchanger is communicated with the feed inlet of the settling kettle. The cold medium discharge port of the rear-stage temperature-raising heat exchanger 4 is communicated with the hot medium feed port of the front-stage temperature-lowering heat exchanger 6 through an intermediate connecting pipeline 10. And a heat medium discharge hole of the rear-stage cooling heat exchanger 7 is communicated with a feed hole of the heat medium water storage tank 1 through a recovery pipeline 11.
A water delivery pump 12 is arranged on the water outlet pipeline 9. The outlet pipe 9 is provided with a port 13 for connection to a cleaning pipe.
A liquid level meter 14 and a thermometer 15 are respectively arranged on the hot water storage tank 1. And a water replenishing pipeline 16 communicated with the purified water pipe is also arranged on the heat medium water storage tank 1.
A material liquid thermometer 17 is respectively arranged on a high-temperature material liquid inlet and outlet pipeline of a hydrogenation reaction system of each stage of temperature rising heat exchanger, and a temperature rising water thermometer 18 is respectively arranged on the temperature rising middle pipeline 5.
The pipelines of the boiler demineralized water inlet and outlet post-stage cooling heat exchanger 7 are respectively provided with a brine thermometer 19, the pipelines of the raw material slurry mixing water inlet and outlet pre-stage cooling heat exchanger 6 are respectively provided with a slurry mixing water thermometer 20, and the cooling intermediate pipeline 8 is provided with a cooling water thermometer 21.
An intermediate temperature gauge 22 is arranged on the intermediate connecting line 10.
The utility model discloses a hydrogenation reactant heat recovery utilizes the use of system is like: the heat medium water (40 ℃, 120 t/h) exchanges heat with the high-temperature material liquid of the hydrogenation reaction system of the front-stage heating heat exchanger 2, the temperature of the heat medium water is increased to 55.1 ℃, and then exchanges heat with the high-temperature material liquid of the other hydrogenation reaction system of the middle-stage heating heat exchanger 3, the temperature of the heat medium water is increased to 75.7 ℃, and the heat energy recovery process is completed. And the heat medium water with the temperature of 75.7 ℃ exchanges heat with the raw material slurry mixing water (40 ℃, 25 t/h) and the boiler desalted water (25 ℃, 35 t/h) of the hydrogenation reaction system in sequence, wherein the temperature of the raw material slurry mixing water is heated from 40 ℃ to 65.9 ℃, the temperature of the boiler desalted water is heated from 25 ℃ to 49.4 ℃, and the heat medium water after heat exchange and temperature reduction returns to the heat medium water storage tank 1 to finish the heat energy utilization process.
Use the utility model discloses a 1.5 tons of steam are practiced thrift every hour to hydrogenation reactant heat recovery utilizes system to annual operating duration 8000 hours, the steam cost can be practiced thrift about 170 ten thousand yuan annually, and energy-conservation and reduce cost's effect is showing.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (8)
1. The utility model provides a hydrogenation reactant heat recycle system, a serial communication port, including heat medium water storage tank, the intensification heat exchanger of at least one-level heat recovery and the cooling heat exchanger of at least one-level heat utilization, heat medium water storage tank passes through outlet conduit and the cold medium feed inlet intercommunication of intensification heat exchanger, the hot medium feed inlet of intensification heat exchanger and the high temperature feed liquid pipeline of hydrogenation reaction system intercommunication, the hot medium discharge gate of intensification heat exchanger and the feed inlet intercommunication of settling kettle, the cold medium discharge gate of intensification heat exchanger passes through intermediate junction pipeline and the hot medium feed inlet intercommunication of cooling heat exchanger, the hot medium discharge gate of cooling heat exchanger passes through the feed inlet intercommunication of recovery pipeline and heat medium water storage tank, set up water pump on outlet conduit, set up level gauge and thermometer on heat medium water storage tank respectively.
2. The hydrogenation reactant heat recycling system as claimed in claim 1, wherein a water replenishing pipeline is further provided on the heating medium water storage tank to communicate with the purified water pipe.
3. The system for recycling the heat of the hydrogenation reactants as claimed in claim 1, wherein a two-stage heat exchanger for heat energy utilization is disposed in the system for recycling the heat of the hydrogenation reactants, the former stage heat exchanger exchanges heat with the slurry-mixing water of the hydrogenation reaction to raise the temperature, the latter stage heat exchanger exchanges heat with the boiler desalted water of the hydrogenation reaction to raise the temperature, the two stages of heat exchangers are disposed with intermediate cooling pipes connected in series, one end of the intermediate cooling pipe is communicated with the heat medium outlet of the former stage heat exchanger, and the other end of the intermediate cooling pipe is communicated with the heat medium inlet of the latter stage heat exchanger.
4. The hydrogenation reactant heat recycling system as claimed in claim 3, wherein the pipeline for boiler demineralized water to enter and exit the cooling heat exchanger is respectively provided with a brine thermometer, the pipeline for raw material slurry mixing water to enter and exit the cooling heat exchanger is respectively provided with a slurry mixing water thermometer, and the cooling intermediate pipeline is provided with a cooling water thermometer.
5. The system for recycling the heat of the hydrogenation reactants as claimed in claim 1, wherein a three-stage heat recovery warming heat exchanger is arranged in the system, the three-stage warming heat exchangers are connected in series through a warming intermediate pipeline, one end of the warming intermediate pipeline is communicated with a cold medium outlet of a previous stage warming heat exchanger, the other end of the warming intermediate pipeline is communicated with a cold medium inlet of a next stage warming heat exchanger, a hot medium inlet of each stage warming heat exchanger is respectively communicated with a high-temperature material liquid pipeline of the hydrogenation reaction system, and a hot medium outlet of each stage warming heat exchanger is respectively communicated with inlets of the settling kettles.
6. The system for recycling heat of hydrogenation reactants as claimed in claim 1, wherein a feed liquid thermometer is respectively arranged on a high-temperature feed liquid inlet and outlet pipeline of the hydrogenation reaction system of each temperature-rising heat exchanger, and a temperature-rising water thermometer is respectively arranged on a temperature-rising intermediate pipeline.
7. The hydrogenation reactant heat recovery system as claimed in claim 1, wherein an intermediate thermometer is provided on the intermediate connecting conduit.
8. The hydrogenation reactant heat recovery system of claim 1, wherein an interface to a purge line is provided on the outlet conduit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023192522.6U CN213955673U (en) | 2020-12-27 | 2020-12-27 | Hydrogenation reactant heat recycling system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023192522.6U CN213955673U (en) | 2020-12-27 | 2020-12-27 | Hydrogenation reactant heat recycling system |
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| Publication Number | Publication Date |
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| CN213955673U true CN213955673U (en) | 2021-08-13 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202023192522.6U Active CN213955673U (en) | 2020-12-27 | 2020-12-27 | Hydrogenation reactant heat recycling system |
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| CN (1) | CN213955673U (en) |
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- 2020-12-27 CN CN202023192522.6U patent/CN213955673U/en active Active
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