CN201988202U - Ammonia evaporating system in process of preparing acrylonitrile through propylene ammoniation and oxidation - Google Patents
Ammonia evaporating system in process of preparing acrylonitrile through propylene ammoniation and oxidation Download PDFInfo
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- CN201988202U CN201988202U CN 201120110251 CN201120110251U CN201988202U CN 201988202 U CN201988202 U CN 201988202U CN 201120110251 CN201120110251 CN 201120110251 CN 201120110251 U CN201120110251 U CN 201120110251U CN 201988202 U CN201988202 U CN 201988202U
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Abstract
The utility model relates to an ammonia evaporating system in the process of preparing the acrylonitrile through propylene ammoniation and oxidation. The ammonia evaporating system comprises an ammonia evaporator which is connected with a liquid ammonia storage tank, wherein a gaseous phase outlet of the ammonia evaporator is connected with an ammonia superheater, and a liquid phase outlet of the ammonia evaporator is connected with a liquid ammonia draining trough; a low-pressure steam pipeline is connected with the liquid ammonia draining trough, the gaseous phase outlet is arranged at the top of the liquid ammonia draining trough, and the liquid phase outlet of the liquid ammonia draining trough is connected with a recovery device. The ammonia evaporating system is characterized in that the gaseous phase outlet at the top of the liquid ammonia draining trough is connected with a follow-up working procedure of propylene oxidation for preparing the acrylonitrile, and an automatic liquid level regulating valve for the liquid ammonia draining trough is arranged between the liquid phase outlet of the liquid ammonia draining trough and the recovery device and can automatically control the liquid level of the liquid ammonia draining trough; and an automatic liquid draining flow regulating valve is arranged between an inlet of the liquid ammonia draining trough and the liquid phase outlet of the ammonia evaporator and automatically controls the flow of the liquid ammonia. Compared with the prior art, the ammonia evaporating system carries out the continuous and automatic control on the liquid drainage of the ammonia evaporator by additionally arranging the automatic liquid level regulating valve for the liquid ammonia draining trough and the automatic liquid draining flow regulating valve and eliminates the ponding in the ammonia evaporator; and the ammonia evaporator has good evaporating effect.
Description
Technical field
The utility model relates to chemical producing system, refers to that specifically a kind of propylene ammoxidation prepares the ammonia vapo(u)rization system in the acrylonitrile process.
Background technology
Acrylonitrile is a purposes Organic Chemicals very widely, occupies critical role in international chemical industry raw materials market.Present large-scale acrylonitrile installation all adopts propylene, ammonia oxidation explained hereafter acrylonitrile, and this method has raw material sources wide and inexpensive, easy and goes on foot advantages such as synthetic, that production cost is low.Whole process of production is divided into synthesis procedure and refining step.In synthesis procedure, reaction raw materials enters reactor by the bottom, liquid propene through propylene vapo(u)rization system, liquefied ammonia through ammonia vapo(u)rization system evaporation heating back with enter blender through air saturated and that heat and mix; Then, enter reactor again, under catalyst action, react with certain reaction temperature and pressure.
Among the aforesaid propylene nitrile preparation technology, the employed ammonia vapo(u)rization system of prior art as shown in Figure 2.
Liquefied ammonia 1 ' enters ammonia evaporator 3 ' back in pressure 0.47MPaG, 7 ℃ of evaporations down of temperature, and the liquid level of ammonia evaporator 3 ' is by automatic regulating valve 2 ' control.After ammonia evaporator 3 ' evaporation, it is overheated that vapor phase ammonia 13 ' enters ammonia superheater 14 ', and the employed thermal source 16 ' of ammonia superheater is a low-pressure steam, and the flow of low-pressure steam is by automatic regulating valve 17 ' control, and steam condensate 18 ' is sent the battery limit (BL).Unevaporated liquefied ammonia 4 ' is interrupted by the artificial valve of operation 19 ' and enters ammonia sump pit 6 ' and send to and carry out double evaporation-cooling in the ammonia evaporator 3 '.Pressure in the ammonia sump pit 6 ' is that 0.47MpaG, temperature are 65 ℃.Vapor phase ammonia 12 ' returns ammonia evaporator 3 ' in the ammonia sump pit, and bottom discharge opeing 7 ' is discharged the battery limit (BL) by the artificial valve 20 ' of operation.Ammonia evaporator tank 6 ' the employed heat medium is a low-pressure steam 9 ', and the low-pressure steam amount is controlled by the artificial valve 21 ' of operation, and steam condensate 10 ' is sent the battery limit (BL).
Because charging liquefied ammonia contains small amount of moisture, so have low amounts of water in the actual production process and be accumulated in the ammonia evaporator 3 ', cause the ammonia evaporator evaporation effect bad.
Summary of the invention
Technical problem to be solved in the utility model is that the present situation at prior art provides a kind of and can continuous draining prepares ammonia vapo(u)rization system in the acrylonitrile process with the propylene ammoxidation of water accumulating volume in effective control ammonia evaporator.
The utility model solves the problems of the technologies described above the technical scheme that is adopted: this propylene ammoxidation prepares the ammonia vapo(u)rization system in the acrylonitrile process, comprises
Ammonia evaporator evaporates liquefied ammonia, and the ammonia evaporator feed(raw material)inlet connects the liquefied ammonia storage tank; The gaseous phase outlet of ammonia evaporator connects following ammonia superheater, and the liquid phase outlet of ammonia evaporator connects following ammonia sump pit;
The ammonia superheater, vapor phase ammonia is heated, the inlet of ammonia superheater connects the gaseous phase outlet of ammonia evaporator (3), for providing the low-pressure steam pipeline of thermal source, the ammonia superheater is connected the upper end of ammonia superheater, and described low-pressure steam pipeline is provided with the gas ammonia automatic temperature control valve of temperature in the automatic control ammonia superheater, the gaseous phase outlet of ammonia superheater connects the next procedure that the propylene ammoxidation prepares acrylonitrile, and the steam condensate outlet of ammonia superheater connects the steam condensate retracting device;
The ammonia sump pit, be used for reclaiming and the unevaporated liquefied ammonia of double evaporation-cooling ammonia evaporator, the inlet of ammonia sump pit connects the liquid phase outlet of ammonia evaporator, for providing the low-pressure steam pipeline of thermal source, the ammonia sump pit connects the ammonia sump pit, the top of ammonia sump pit is provided with gaseous phase outlet, the liquid phase outlet of ammonia sump pit connects retracting device, and the steam condensate outlet of ammonia sump pit connects the steam condensate retracting device;
It is characterized in that: the gaseous phase outlet at described ammonia sump pit top connects the next procedure that described propylene ammoxidation prepares acrylonitrile, is provided with the ammonia sump pit liquid level automatic regulating valve that can control liquid level in the described ammonia sump pit automatically between the liquid phase outlet of described ammonia sump pit and the retracting device; Be provided with the draining flow automatic regulating valve of automatic control liquefied ammonia flow between the inlet of described ammonia sump pit and the outlet of the liquid phase of described ammonia evaporator.
Described gas ammonia automatic temperature control valve, ammonia sump pit liquid level automatic regulating valve all are connected central DCS control system with the draining flow automatic regulating valve.
Compared with prior art, the utility model is the setting of second magnetic valve and the 3rd magnetic valve by the control loop of setting up the ammonia sump pit, can control continuously and automatically the discharge opeing of ammonia evaporator, eliminated the ponding in the ammonia evaporator, fully improve the efficient of ammonia evaporator, guaranteed the quality of vapor phase ammonia, the evaporation effect of ammonia evaporator is good.
Description of drawings
Fig. 1 is the planar structure schematic diagram of the utility model embodiment;
Fig. 2 is the planar structure schematic diagram of ammonia vapo(u)rization system in the utility model background technology.
The specific embodiment
Embodiment describes in further detail the utility model below in conjunction with accompanying drawing.
1-liquefied ammonia storage tank; 2-ammonia evaporator fluid level control valve; The 3-ammonia evaporator; The outlet of 4-ammonia evaporator liquid phase; 5-draining flow automatic regulating valve; 6-ammonia sump pit; The outlet of 7-ammonia sump pit liquid phase; 8-ammonia sump pit liquid level automatic regulating valve; 9-low-pressure steam pipeline; 10-steam condensate retracting device; 11-sump pit automatic temperature control valve; 12-ammonia sump pit top gaseous phase outlet; 13-ammonia evaporator gaseous phase outlet; 14-ammonia superheater; The next procedure that 15-propylene ammoxidation prepares acrylonitrile; 16-low-pressure steam pipeline; 17-gas ammonia automatic temperature control valve; 18-steam condensate retracting device.
As shown in Figure 1, be the example explanation to produce 260000 tons of acrylonitrile installations per year, the ammonia vapo(u)rization system that this propylene oxidation prepares in the acrylonitrile process comprises:
Above-mentioned each automatic regulating valve all connects the central DCS control system of acrylonitrile installation.
The operation principle of above-mentioned ammonia vapo(u)rization system is as follows:
The liquefied ammonia that contains ammonia 99.5wt%, water 0.5wt% is sent into ammonia evaporator 3 with 17000kg/hr, at pressure is 0.22～0.37MPa, 7 ℃ of evaporations down of temperature, the vapor phase ammonia that ammonia evaporator 3 obtains is sent to ammonia superheater 14, and it is the outlet temperature that thermal source passes through gas ammonia automatic temperature control valve 17 control vapor phase ammonias that ammonia superheater 14 adopts low-pressure steam.Hydrops in the ammonia evaporator 3 enters ammonia sump pit 6 by draining flow autocontrol valve 5 control liquefied ammonia with the flow of 400kg/hr.The operating pressure of ammonia sump pit 6 is that 0.2～0.4MPa, temperature are 60～70 ℃.Thereby by the temperature in the flow control ammonia sump pit 6 of sump pit automatic temperature control valve 11 control low-pressure steams, the design load of this low-pressure steam flow is 275kg/hr.The logical ammonia sump pit liquid level automatic regulating valve 8 of ammonia sump pit 6 bottom blow-downs is controlled, and normal value is about 80kg/hr, and the vapor phase ammonia that the top obtains is sent to the next procedure 15 that the propylene ammoxidation prepares acrylonitrile after gathering with vapor phase ammonia from ammonia evaporator 3.
Claims (2)
1. a propylene ammoxidation prepares the ammonia vapo(u)rization system in the acrylonitrile process, comprises
Ammonia evaporator (3) evaporates liquefied ammonia, and ammonia evaporator (3) feed(raw material)inlet connects liquefied ammonia storage tank (1); The gaseous phase outlet of ammonia evaporator (3) connects following ammonia superheater (14), and the liquid phase outlet of ammonia evaporator (3) connects following ammonia sump pit (6);
Ammonia superheater (14), vapor phase ammonia is heated, the inlet of ammonia superheater (14) connects the gaseous phase outlet of ammonia evaporator (3), for providing the low-pressure steam pipeline (16) of thermal source, ammonia superheater (14) is connected on the ammonia superheater (14), and described low-pressure steam pipeline (16) is provided with the gas ammonia automatic temperature control valve (17) of temperature in the automatic control ammonia superheater, the gaseous phase outlet of ammonia superheater (14) connects the next procedure (15) that the propylene ammoxidation prepares acrylonitrile, and the steam condensate outlet of ammonia superheater (14) connects steam condensate retracting device (18);
Ammonia sump pit (6), be used for reclaiming and the unevaporated liquefied ammonia of double evaporation-cooling ammonia evaporator, the inlet of ammonia sump pit (6) connects the liquid phase outlet of ammonia evaporator (3), for providing the low-pressure steam pipeline (9) of thermal source, the ammonia sump pit connects ammonia sump pit (6), the top of ammonia sump pit (6) is provided with gaseous phase outlet, the liquid phase outlet of ammonia sump pit (6) connects retracting device (7), and the steam condensate outlet of ammonia sump pit (6) connects steam condensate retracting device (10);
It is characterized in that: the gaseous phase outlet at described ammonia sump pit (6) top connects the next procedure (15) that described propylene oxidation prepares acrylonitrile, is provided with the ammonia sump pit liquid level automatic regulating valve (8) that can control the interior liquid level of described ammonia sump pit (6) automatically between the liquid phase outlet of described ammonia sump pit (6) and the retracting device (7); Be provided with the draining flow automatic regulating valve (5) of automatic control liquefied ammonia flow between the liquid phase outlet of the inlet of described ammonia sump pit (6) and described ammonia evaporator (3).
2. propylene ammoxidation according to claim 1 prepares the ammonia vapo(u)rization system in the acrylonitrile process, it is characterized in that described gas ammonia automatic temperature control valve (17), ammonia sump pit liquid level automatic regulating valve (8) and draining flow automatic regulating valve (5) all are connected central DCS control system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120110251 CN201988202U (en) | 2011-04-11 | 2011-04-11 | Ammonia evaporating system in process of preparing acrylonitrile through propylene ammoniation and oxidation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120110251 CN201988202U (en) | 2011-04-11 | 2011-04-11 | Ammonia evaporating system in process of preparing acrylonitrile through propylene ammoniation and oxidation |
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| CN201988202U true CN201988202U (en) | 2011-09-28 |
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| CN 201120110251 Expired - Lifetime CN201988202U (en) | 2011-04-11 | 2011-04-11 | Ammonia evaporating system in process of preparing acrylonitrile through propylene ammoniation and oxidation |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107253705A (en) * | 2017-06-26 | 2017-10-17 | 贵州芭田生态工程有限公司 | The method for discharging pollution and its device of ammonia vapo(u)rization system in a kind of double pressurized method production nitric acid |
| CN109772234A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | Unstripped gas feed system for ammoxidation of propylene reactor |
| CN115518515A (en) * | 2022-09-14 | 2022-12-27 | 山东莱钢永锋钢铁有限公司 | Coal-fired boiler denitration system improvement method |
-
2011
- 2011-04-11 CN CN 201120110251 patent/CN201988202U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107253705A (en) * | 2017-06-26 | 2017-10-17 | 贵州芭田生态工程有限公司 | The method for discharging pollution and its device of ammonia vapo(u)rization system in a kind of double pressurized method production nitric acid |
| CN109772234A (en) * | 2017-11-14 | 2019-05-21 | 中国石油化工股份有限公司 | Unstripped gas feed system for ammoxidation of propylene reactor |
| JP2021505534A (en) * | 2017-11-14 | 2021-02-18 | 中国石油化工股▲ふん▼有限公司 | Supply gas supply system for propylene ammoxidation reactor |
| JP7134232B2 (en) | 2017-11-14 | 2022-09-09 | 中国石油化工股▲ふん▼有限公司 | Feed gas supply system for propylene ammoxidation reactor |
| CN109772234B (en) * | 2017-11-14 | 2024-01-05 | 中国石油化工股份有限公司 | Feed gas feed system for propylene ammoxidation reactor |
| CN115518515A (en) * | 2022-09-14 | 2022-12-27 | 山东莱钢永锋钢铁有限公司 | Coal-fired boiler denitration system improvement method |
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| C14 | Grant of patent or utility model | ||
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| CP01 | Change in the name or title of a patent holder |
Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Patentee after: Sinopec Corp. Patentee after: SINOPEC Ningbo Engineering Company Limited Patentee after: SINOPEC Ningbo Technology Research Institute Co., Ltd. Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Patentee before: Sinopec Corp. Patentee before: Sinopec Ningbo Engineering Co., Ltd. Patentee before: Sinopec Ningbo Institute of Technology |
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Granted publication date: 20110928 |
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| CX01 | Expiry of patent term |