CN218853480U - Urea production system for comprehensively utilizing waste heat of steam condensate - Google Patents
Urea production system for comprehensively utilizing waste heat of steam condensate Download PDFInfo
- Publication number
- CN218853480U CN218853480U CN202223576899.0U CN202223576899U CN218853480U CN 218853480 U CN218853480 U CN 218853480U CN 202223576899 U CN202223576899 U CN 202223576899U CN 218853480 U CN218853480 U CN 218853480U
- Authority
- CN
- China
- Prior art keywords
- communicated
- stage
- tower
- inlet
- tank
- 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.)
- Active
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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a urea production system for comprehensively utilizing waste heat of steam condensate, which comprises a stripping tower, a pool condenser, a synthesis tower, a rectifying tower, a flash tank, a urine tank, a first-stage evaporator, a second-stage evaporator and a granulation tower which are connected with each other, wherein a water outlet and a water return port of a low-pressure steam drum are correspondingly communicated with a heat exchange inlet and a heat exchange outlet of the pool condenser; the rectification tower is communicated with a rectification separation tank, and the rectification separation tank is communicated with a deaerator through a rectification separation pump; the first-stage evaporator is communicated with the first-stage separation tank, and the first-stage separation tank is communicated with the deaerator through a first-stage separation pump; the second-stage evaporator is communicated with the low-pressure steam drum, and the second-stage separation tank is communicated with the low-pressure steam drum through a second-stage separation pump; the deaerator is communicated with the steam boiler and the temperature and pressure reducing device in sequence; the temperature and pressure reduction device is respectively communicated with the rectifying tower, the first-stage evaporator and the second-stage evaporator. Has the advantages that: the problem of condensate flash distillation cooling is solved, heat loss has been avoided.
Description
The technical field is as follows:
the utility model relates to a urea production field especially relates to a urea production system of steam condensate waste heat comprehensive utilization.
The background art comprises the following steps:
in the process of urea production, the content of urea in liquid components from a synthesis tower is about 30 percent generally, and the urea is sent for granulation only after being concentrated to more than 99 percent step by step, steam heating is generally needed in the concentration process to change light components in the liquid components into gas phase, so that the concentration of urine is improved, the urine is heated by the steam and is changed into condensate, and the steam heating process utilizes the latent heat of the steam, so that the temperature of the condensate is still high and is basically more than 130 ℃. The heated steam condensate is sent to a condensate big tank in a normal pressure state, the temperature of the condensate can be reduced to be within 100 ℃ due to the flash evaporation effect generated by the reduction of the pressure, the flashed steam is sent to the condensate big tank after being cooled by a heat exchanger, and then is sent to a boiler device through a delivery pump to be used as the water supplement of the boiler, the general temperature of the condensate big tank is 95 ℃, which is equivalent to the waste of the heat energy of the condensate from 130 ℃ to 95 ℃, and a certain amount of circulating water can be consumed for reducing the temperature of the condensate.
The utility model has the following contents:
an object of the utility model is to provide a solve the problem that the steam condensate flash distillation cooling leads to calorific loss, make full use of condensate heat steam condensate waste heat comprehensive utilization's urea production system.
The utility model discloses by following technical scheme implement: the urea production system comprehensively utilizing the waste heat of steam condensate comprises a stripping tower, a pool condenser, a synthesis tower, a rectifying tower, a flash tank, a urine tank, a first-stage evaporator, a second-stage evaporator and a granulation tower which are connected with each other, wherein a gas outlet of the stripping tower is communicated with an inlet of the synthesis tower through the pool condenser; a water outlet and a water return port of the low-pressure steam drum are correspondingly communicated with a heat exchange inlet and a heat exchange outlet of the pool type condenser; the device is characterized in that a condensate port of the rectifying tower is communicated with an inlet of a rectifying and separating tank through a pipeline, and an outlet of the rectifying and separating tank is communicated with an inlet of a deaerator through a rectifying and separating pump; a condensate port of the first-stage evaporator is communicated with an inlet of a first-stage separation tank through a pipeline, and an outlet of the first-stage separation tank is communicated with an inlet of the deaerator through a first-stage separation pump; a condensate port of the second-stage evaporator is communicated with an inlet of a second-stage separation tank through a pipeline, and an outlet of the second-stage separation tank is communicated with a liquid supplementing port of the low-pressure steam drum through a second-stage separation pump; the deaerator is communicated with the steam boiler and the temperature and pressure reducing device in sequence; and a steam outlet of the temperature and pressure reducing device is respectively communicated with a steam inlet of the rectifying tower, a steam inlet of the first-section evaporator and a steam inlet of the second-section evaporator through pipelines.
Preferably, the gas inlet of the stripping tower is communicated with a carbon dioxide gas source; the gas outlet of the stripping tower is communicated with the gas inlet of the pool condenser; a liquid inlet of the pool condenser is communicated with a liquid ammonia storage tank; the discharge hole of the pool condenser is communicated with the feed inlet of the synthesis tower; an overflow port of the synthesis tower is communicated with a liquid inlet of the stripping tower; the liquid outlet of the stripping tower is communicated with the liquid inlet of the rectifying tower; the rectifying tower, the flash tank, the urine tank, the first-stage evaporator, the second-stage evaporator and the granulation tower are communicated in sequence.
Preferably, a rectification liquid level regulating valve is arranged on a water outlet of the rectification separation pump, and a liquid level sensor of the rectification liquid level regulating valve is arranged on the rectification separation tank; a water outlet of the first-stage separation pump is provided with a first-stage liquid level regulating valve, and a liquid level sensor of the first-stage liquid level regulating valve is arranged on the first-stage separation tank; and a water outlet of the second-stage separation pump is provided with a second-stage liquid level regulating valve, and a liquid level sensor of the second-stage liquid level regulating valve is arranged on the second-stage separation tank.
The utility model has the advantages that: compared with the prior art, the steam condensate of the rectifying tower and the first-stage evaporator is directly sent to the deaerator, is heated by the steam boiler to be used as the heat source of the rectifying tower, the first-stage evaporator and the second-stage evaporator, and the steam condensate of the second-stage evaporator is directly sent to the low-pressure steam pocket to be used as the fluid infusion to replace the fluid infusion from the condensate large tank to the low-pressure steam pocket, so that the problem of flash evaporation and temperature reduction of the condensate is solved, and the heat loss is avoided; meanwhile, the fuel consumption of the steam boiler is reduced, and the utilization rate of heat energy is improved.
Description of the drawings:
fig. 1 is a schematic diagram of the system connection of the present invention.
The specific implementation mode is as follows:
example (b): as shown in fig. 1, the urea production system for comprehensively utilizing the waste heat of steam condensate comprises a stripping tower 1, a pool condenser 2, a synthesis tower 3, a rectifying tower 4, a flash evaporation tank 5, a urine tank 6, a first-stage evaporator 7, a second-stage evaporator 8 and a granulation tower 9 which are connected with each other, wherein an air inlet of the stripping tower 1 is communicated with a carbon dioxide air source 10; the air outlet of the stripping tower 1 is communicated with the air inlet of the pool condenser 2; the liquid inlet of the pool condenser 2 is communicated with a liquid ammonia storage tank 11; the discharge hole of the pool condenser 2 is communicated with the feed inlet of the synthesis tower 3; an overflow port of the synthesis tower 3 is communicated with a liquid inlet of the stripping tower 1; a liquid outlet of the stripping tower 1 is communicated with a liquid inlet of the rectifying tower 4; the rectifying tower 4, the flash evaporation tank 5, the urine tank 6, the first-stage evaporator 7, the second-stage evaporator 8 and the granulation tower 9 are communicated in sequence; a water outlet and a water return port of the low-pressure steam drum 12 are correspondingly communicated with a heat exchange inlet and a heat exchange outlet of the pool type condenser 2; a condensate port of the rectifying tower 4 is respectively communicated with inlets of a condensate tank 13 and a rectifying and separating tank 41 through pipelines, and an outlet of the rectifying and separating tank 41 is communicated with an inlet of a deaerator 14 through a rectifying and separating pump 42; a rectification liquid level regulating valve 43 is arranged on a water outlet of the rectification separation pump 42, and a liquid level sensor of the rectification liquid level regulating valve 43 is arranged on the rectification separation tank 41; a condensate port of the first-stage evaporator 7 is respectively communicated with inlets of the condensate tank 13 and the first-stage separation tank 71 through pipelines, and an outlet of the first-stage separation tank 71 is communicated with an inlet of the deaerator 14 through a first-stage separation pump 72; a water outlet of the first-stage separation pump 72 is provided with a first-stage liquid level regulating valve 73, and a liquid level sensor of the first-stage liquid level regulating valve 73 is arranged on the first-stage separation tank 71; a condensate port of the second-stage evaporator 8 is respectively communicated with inlets of the condensate tank 13 and the second-stage separation tank 81 through pipelines, and an outlet of the second-stage separation tank 81 is communicated with a liquid supplementing port of the low-pressure steam drum 12 through a second-stage separation pump 82; the deaerator 13 is communicated with the steam boiler 15 and the temperature and pressure reducing device 16 in sequence; the steam outlet of the temperature and pressure reducing device 16 is respectively communicated with the steam inlet of the rectifying tower 4, the steam inlet of the first-stage evaporator 7 and the steam inlet of the second-stage evaporator 8 through pipelines.
The working principle is as follows: carbon dioxide gas and liquid ammonia enter the pool condenser 2 to be condensed into ammonium carbamate liquid, the generated heat is removed by water sent by the low-pressure steam drum 12, and low-pressure steam is generated; enabling the ammonium carbamate solution to enter a synthesis tower 3 for producing urea by water shrinkage, and enabling the ammonium carbamate solution to flow out from an overflow port at the top of the synthesis tower 3 from bottom to top; the urea overflowed from the synthesis tower 3 and the methylamine which is not shrunk to generate the urea enter the stripping tower 1, the methylamine which is not shrunk to generate the urea is decomposed in the stripping tower 1 to generate carbon dioxide and ammonia, the carbon dioxide and the ammonia generated by decomposition and the carbon dioxide provided by the carbon dioxide gas source 10 enter the pool condenser 2 again for reaction, and the concentration of the urea in the liquid phase is improved in the process; the liquid phase in the stripping tower 1 enters a rectifying tower 4, a flash evaporation tank 5, a urine tank 6, a first-stage evaporator 7 and a second-stage evaporator 8 in sequence, wherein light components such as ammonia, carbon dioxide, water and the like become gas phase, the concentration of urea in the liquid phase is further improved, the concentration of urea in the liquid reaches 99.5%, and then the liquid phase is sent into a granulation tower 9 for granulation.
The steam condensate of the rectifying tower 4 and the first-stage evaporator 7 is directly sent to the deaerator 14 and is heated by the steam boiler 15 to be used as the heat source of the rectifying tower 4, the first-stage evaporator 7 and the second-stage evaporator 8, so that the problem of flash evaporation and cooling of the condensate is solved, the heat loss is avoided, and meanwhile, the fuel consumption of the steam boiler 15 is reduced; the steam condensate of the two-stage evaporator 8 is directly sent to the low-pressure steam drum 12 to be used as the liquid supplement to replace the liquid supplement from the condensate tank 13 to the low-pressure steam drum 12, so that the problem of flash evaporation and temperature reduction of the condensate is solved, and the heat loss is avoided.
The condensate ports of the rectifying tower 4, the first-stage evaporator 7 and the second-stage evaporator 8 are communicated with the condensate tank 13, so that steam condensate can be sent to the condensate tank 13 when the rectifying separation pump 42, the first-stage separation pump 72 and the second-stage separation pump 82 break down and rush repair is carried out, the stable operation of the system is ensured, and the system can not be shut down due to the faults of the rectifying separation pump 42, the first-stage separation pump 72 and the second-stage separation pump 82.
Claims (3)
1. The urea production system comprehensively utilizing the waste heat of the steam condensate comprises a stripping tower, a pool condenser, a synthesis tower, a rectifying tower, a flash tank, a urine tank, a first-stage evaporator, a second-stage evaporator and a granulation tower which are connected with each other, wherein a gas outlet of the stripping tower is communicated with an inlet of the synthesis tower through the pool condenser; a water outlet and a water return port of the low-pressure steam drum are correspondingly communicated with a heat exchange inlet and a heat exchange outlet of the pool type condenser; the device is characterized in that a condensate port of the rectifying tower is communicated with an inlet of a rectifying and separating tank through a pipeline, and an outlet of the rectifying and separating tank is communicated with an inlet of a deaerator through a rectifying and separating pump; a condensate port of the first-section evaporator is communicated with an inlet of a first-section separation tank through a pipeline, and an outlet of the first-section separation tank is communicated with an inlet of the deaerator through a first-section separation pump; a condensate port of the second-stage evaporator is communicated with an inlet of a second-stage separation tank through a pipeline, and an outlet of the second-stage separation tank is communicated with a liquid supplementing port of the low-pressure steam drum through a second-stage separation pump; the deaerator is communicated with the steam boiler and the temperature and pressure reducing device in sequence; and a steam outlet of the temperature and pressure reducing device is respectively communicated with a steam inlet of the rectifying tower, a steam inlet of the first-section evaporator and a steam inlet of the second-section evaporator through pipelines.
2. The system for producing urea by comprehensively utilizing steam condensate waste heat according to claim 1, wherein an air inlet of the stripping tower is communicated with a carbon dioxide air source; the gas outlet of the stripping tower is communicated with the gas inlet of the pool condenser; a liquid inlet of the pool condenser is communicated with a liquid ammonia storage tank; the discharge hole of the pool condenser is communicated with the feed inlet of the synthesis tower; an overflow port of the synthesis tower is communicated with a liquid inlet of the stripping tower; the liquid outlet of the stripping tower is communicated with the liquid inlet of the rectifying tower; the rectifying tower, the flash tank, the urine tank, the first-stage evaporator, the second-stage evaporator and the granulation tower are communicated in sequence.
3. The urea production system for comprehensively utilizing the waste heat of the steam condensate as claimed in claim 2, wherein a rectification liquid level regulating valve is arranged on a water outlet of the rectification separation pump, and a liquid level sensor of the rectification liquid level regulating valve is arranged on the rectification separation tank; a water outlet of the first-stage separation pump is provided with a first-stage liquid level regulating valve, and a liquid level sensor of the first-stage liquid level regulating valve is arranged on the first-stage separation tank; and a water outlet of the second-stage separation pump is provided with a second-stage liquid level regulating valve, and a liquid level sensor of the second-stage liquid level regulating valve is arranged on the second-stage separation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223576899.0U CN218853480U (en) | 2022-12-30 | 2022-12-30 | Urea production system for comprehensively utilizing waste heat of steam condensate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223576899.0U CN218853480U (en) | 2022-12-30 | 2022-12-30 | Urea production system for comprehensively utilizing waste heat of steam condensate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218853480U true CN218853480U (en) | 2023-04-14 |
Family
ID=87374986
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223576899.0U Active CN218853480U (en) | 2022-12-30 | 2022-12-30 | Urea production system for comprehensively utilizing waste heat of steam condensate |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218853480U (en) |
-
2022
- 2022-12-30 CN CN202223576899.0U patent/CN218853480U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111437619A (en) | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method | |
| CN105366751A (en) | Energy-saving environment-friendly integrated recycling and utilization method of coal chemical gasification washing black water high-temperature flashing steam | |
| CN218853480U (en) | Urea production system for comprehensively utilizing waste heat of steam condensate | |
| CN218642708U (en) | Intelligent energy-saving and emission-reducing system of wine cooler | |
| CN101913669A (en) | Multi-effect energy-saving ammonia recovery process and device | |
| CN109437239A (en) | The low temperature position exhaust heat recovering method and device of process are absorbed in a kind of acid-making process | |
| CN108726536A (en) | A kind of system and method for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat | |
| CN212532809U (en) | Pre-concentration device of urea low-pressure system | |
| CN112239390B (en) | Ethylene cryogenic recovery system | |
| CN208732629U (en) | A kind of system for producing liquefied ammonia using soda manufacture process steam condensation fluid residual heat | |
| CN212818177U (en) | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system | |
| CN110388638B (en) | Steam heat energy recycling process in urea production by carbon dioxide gas stripping method | |
| CN106679243B (en) | Refrigerating system capable of reducing liquid ammonia consumption | |
| CN209507605U (en) | The low temperature position waste-heat recovery device of process is absorbed in a kind of acid-making process | |
| CN203238198U (en) | System for utilizing waste heat of byproduct low-pressure steam in coal ethylene glycol process | |
| CN203440268U (en) | Heat recovery device in urea production device | |
| CN111717948A (en) | Coking gas phase circulation ammonia distillation process and device | |
| CN111056580A (en) | Vinyl sulfate waste water treatment and recovery system | |
| CN201801393U (en) | Multiple-effect equipment used in energy-saving ammonia recovering process | |
| CN210193454U (en) | A splitter for waste water evaporation retrieval and utilization | |
| CN220276335U (en) | System of composite steam jet vacuum pump unit utilizing green energy | |
| CN215809432U (en) | Waste heat recovery utilizes device in concentrated nitric acid production | |
| CN217367195U (en) | MTO grade methanol production system | |
| CN221036254U (en) | Heat pump system for preparing high-temperature steam by using chemical waste heat wastewater or waste steam | |
| CN219272184U (en) | Rectifying column top methanol steam heat recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |