阅读说明：本技术 一种提高氢酯比的装置及应用方法 (Device for improving hydrogen-ester ratio and application method ) 是由 张刚 张向凯 曹洪刚 郭栋 张海永 陈永刚 于 2020-07-21 设计创作，主要内容包括：一种提高氢酯比的装置及应用方法是煤制乙二醇操作技术,它通过增加一套换热系统,使加氢系统进料由原单段进料改为双段进料,达到提高氢气与乙二酸二甲酯的摩尔比的目的,它包括预热器、循环气加热器、过滤器、气气换热器、冷却器、冷凝器、气液分离器、第一高效喷头、第二高效喷头、瓷球、除沫器,所述预热器与循环气加热器由管道连接,循环气加热器由管道与过滤器连接；所述过滤器由管程与气气换热器连接；气气换热器与冷却器由管道连接；冷却器与冷凝器由管道连接；冷凝器与气液分离器由管道连接。(A device for improving the hydrogen-ester ratio and an application method thereof are coal-to-ethylene glycol operation technologies, a set of heat exchange system is added, so that the feeding of a hydrogenation system is changed from the original single-section feeding into the double-section feeding, and the purpose of improving the molar ratio of hydrogen to dimethyl oxalate is achieved, the device comprises a preheater, a circulating gas heater, a filter, a gas-gas heat exchanger, a cooler, a condenser, a gas-liquid separator, a first high-efficiency spray head, a second high-efficiency spray head, ceramic balls and a demister, wherein the preheater is connected with the circulating gas heater through a pipeline, and the circulating gas heater is connected with the filter through a pipeline; the filter is connected with the gas-gas heat exchanger through a tube pass; the gas-gas heat exchanger is connected with the cooler through a pipeline; the cooler is connected with the condenser through a pipeline; the condenser is connected with the gas-liquid separator through a pipeline.)

1. The utility model provides an improve device of hydrogen ester ratio, it includes pre-heater (1), circulation gas heater (2), filter (3), gas-gas heat exchanger (4), cooler (5), condenser (6), vapour and liquid separator (7), first high-efficient shower nozzle (8), second high-efficient shower nozzle (9), porcelain ball (10), demister (11), characterized by: the preheater (1) is connected with the circulating gas heater (2) through a pipeline, and the circulating gas heater (2) is connected with the filter (3) through a pipeline; the filter (3) is connected with the gas-gas heat exchanger (4) through a tube pass; the gas-gas heat exchanger (4) is connected with the cooler (5) through a pipeline; the cooler (5) is connected with the condenser (6) through a pipeline; the condenser (6) is connected with the gas-liquid separator (7) through a pipeline; the gas-liquid separator (7) is connected with a demister (11); the first spray head (8) and the second spray head (9) are connected to the middle pipelines of the preheater (1) and the circulating gas heater (2); a ceramic ball (10) is arranged in the filter (3).

2. The apparatus of claim 1, wherein: the diameter of the preheater (1) is 700-800mm, the length is 4000-5000mm, the design pressure of a tube pass is 2.8-3.8MPa, the preheater is fixed by a steel structure and is vertically arranged; the diameter of the circulating gas heater (2) is 1500-1800mm, the length is 9000-11000mm, the design pressure of a tube pass is 2.8-3.8MPa, and the circulating gas heater (2) is fixed on a frame by a saddle-type support; the diameter of the filter (3) is 3000-3500mm, the length is 9000-10000mm, the design pressure of a tube side is 2.8-3.8MPa, the filter (3) is fixed on the support by a skirt, and the bottom of the filter (3) is provided with a liquid discharge port; the diameter of the gas-gas heat exchanger (4) is 1800-2000mm, the length is 12000-15000mm, the design pressure of a tube pass is 2.8-3.8MPa, and the gas-gas heat exchanger (4) is fixed on a frame by a saddle-type support; the diameter of the cooler (5) is 1800-2000mm, the length is 10000-13000mm, the design pressure of a tube pass is 2.8-3.8MPa, and the cooler (5) is fixed on the frame by a saddle type support; the diameter of the condenser (6) is 1800-2000mm, the length is 10000-13000mm, the design pressure of a tube side is 2.8-3.8MPa, and the condenser (6) is fixed on the frame by a saddle type support; the diameter of the gas-liquid separator (7) is 2200-2500mm, the length is 8000-12000mm, the design pressure of the tube side is 2.8-3.8MPa, the gas-liquid separator (7) is fixed on the ground by a saddle type support, the bottom of the gas-liquid separator (7) is provided with a liquid discharge port, and the upper part of the gas-liquid separator is provided with a vent pipeline.

3. The application method of the device for increasing the hydrogen-ester ratio as claimed in claim 1, which is characterized in that: after a circulating gas phase is mixed with preheated dimethyl oxalate through a first set of cooler and a gas-gas heat exchanger, the gas phase enters a gas-gas heat exchanger tube pass after reaction through a heater, is cooled by a cooler tube pass and is condensed by a condenser, the gas phase enters a gas-liquid separator for gas-liquid separation, the gas phase returns to an inlet of a compressor, and a liquid phase is sent to a subsequent system; the specific method is that dimethyl oxalate is preheated in a preheater (1), enters a circulating gas heater (2) through a first high-efficiency spray head (8) and a second high-efficiency spray head (9) on a pipeline, the mixed gas of dimethyl oxalate and hydrogen enters a filter (3) after being heated, enters a reactor after impurities are filtered by ceramic balls (10) in the filter (3), glycol is produced after reaction, the glycol and the circulating gas enter a tube pass of a gas-gas heat exchanger (4), then the ethylene glycol, the circulating gas and the circulating hydrogen gas from the cooler (5) exchange heat, then the ethylene glycol, the circulating gas and the circulating hydrogen gas enter the cooler (5) for heat exchange with the circulating hydrogen gas from the previous system, then the ethylene glycol, the circulating gas and the circulating hydrogen gas enter the condenser (6) and are cooled by cooling water and then enter the gas-liquid separator (7), then the ethylene glycol liquid drops are removed by a gas-liquid separator (7) and a demister (11), and the hydrogen is recycled.

4. The parameters of the application method of the device for increasing the hydrogen-ester ratio as claimed in claim 3, wherein: the circulation volume of the hydrogenation system is 500000 Nm/h; the molar ratio of hydrogen to oxalate was 100, 125, respectively; the catalyst bed temperature was maintained at 185 ℃ at 90% loading and the hot spot temperature was reduced by 5-10 ℃.

Technical Field

The invention relates to an operation technology for preparing ethylene glycol from coal, in particular to a device for improving hydrogen-ester ratio and an application method.

Background

The key operation control parameter of the hydrogenation system of the coal-to-ethylene glycol technology is the molar ratio of hydrogen to dimethyl oxalate, which is required to be controlled to be more than 80, but in the original hydrogenation system, the molar ratio can not reach the design condition, which causes great difficulty in operation of the hydrogenation system, short service life of the catalyst and the like, and because the oxalate firstly passes through the former series, the load of the former series is too high, and then passes through the latter series after reaction, the latter series basically does not react (no hot spot temperature) or generates side reaction.

Disclosure of Invention

The invention aims to provide a device for improving the hydrogen-ester ratio and an application method, which change the feeding of a hydrogenation system from the original single-section feeding into the double-section feeding by adding a set of heat exchange system to achieve the aim of improving the molar ratio of hydrogen to dimethyl oxalate; the filter is connected with the gas-gas heat exchanger through a tube pass; the gas-gas heat exchanger is connected with the cooler through a pipeline; the cooler is connected with the condenser through a pipeline; the condenser is connected with the gas-liquid separator through a pipeline.

And the gas-liquid separator is connected with a demister.

The first spray head and the second spray head are connected to the intermediate pipelines of the preheater and the circulating gas heater.

And a ceramic ball is arranged in the filter.

The diameter of the preheater is 700-800mm, the length is 4000-5000mm, the design pressure of a tube pass is 2.8-3.8MPa, and the preheater is fixed by a steel structure and is vertically arranged; the diameter of the circulating gas heater is 1500-1800mm, the length is 9000-11000mm, the design pressure of a tube pass is 2.8-3.8MPa, and the circulating gas heater is fixed on the frame by a saddle type support; the diameter of the filter is 3000-3500mm, the length is 9000-10000mm, the design pressure of a tube side is 2.8-3.8MPa, the filter is fixed on the support by a skirt, and the bottom of the filter is provided with a liquid discharge port; the diameter of the gas-gas heat exchanger is 1800-2000mm, the length is 12000-15000mm, the design pressure of a tube pass is 2.8-3.8MPa, and the gas-gas heat exchanger is fixed on the frame by a saddle type support; the diameter of the cooler is 1800-2000mm, the length is 10000-13000mm, the design pressure of a tube side is 2.8-3.8MPa, and the cooler is fixed on a frame by a saddle type support; the condenser has the diameter of 1800-2000mm, the length of 10000-13000mm and the design pressure of a tube side of 2.8-3.8MPa, and is fixed on a frame by a saddle type support; the diameter of the gas-liquid separator is 2200-2500mm, the length is 8000-12000mm, the design pressure of the tube side is 2.8-3.8MPa, the gas-liquid separator is fixed on the ground by a saddle type support, the bottom of the gas-liquid separator is provided with a liquid discharging port, and the upper part of the gas-liquid separator is provided with a vent pipeline.

The application method of the invention comprises the following steps: after the circulating gas phase is mixed with preheated dimethyl oxalate through a first set of cooler and a gas-gas heat exchanger, the mixture is reacted through a heater, then enters a gas-gas heat exchanger tube pass, a cooler tube pass for cooling and a condenser for condensing, enters a gas-liquid separator for gas-liquid separation, the gas phase returns to the inlet of a compressor, and the liquid phase is sent to a subsequent system.

The specific operation method comprises the steps that dimethyl oxalate is preheated in a preheater and then enters a circulating gas heater through a first high-efficiency spray head and a second high-efficiency spray head on a pipeline, mixed gas of the dimethyl oxalate and hydrogen enters a filter after being heated, impurities are filtered out through ceramic balls in the filter and then enter a reactor, ethylene glycol is produced after reaction, the ethylene glycol and the circulating gas enter a gas-gas heat exchanger tube pass, then the ethylene glycol and the circulating gas exchange heat with circulating hydrogen gas from a cooler, enter the cooler tube pass and exchange heat with the circulating hydrogen gas from a front system, enter a condenser, are cooled by cooling water, enter a gas-liquid separator, and then are subjected to gas-liquid separator and demister to remove ethylene glycol liquid drops, so that the hydrogen is recycled.

Due to the increase of the system resistance, the circulation volume of the hydrogenation system is 500000 Nm/h; therefore, the space velocity after hydrogenation is reduced, and the pressure on the lower catalyst in the reactor tube can be reduced, thereby avoiding the crushing of the lower catalyst.

After the method is applied, the dimethyl oxalate is divided into two parts which are respectively subjected to the front and back series, and under the condition that the circulation volume is reduced to 500000 Nm/h, the molar ratio of hydrogen to oxalate is respectively 100 and 125. The optimal hydrogen-ester ratio required by the system is more than 80, and the rotation speed is reduced at the later stage, wherein the hydrogen-ester ratio is respectively 90-120 and 90-120; at lower rotational speeds, the requirements of the present day can therefore already be met.

After the method is applied, after the catalyst enters a hydrogenation reactor, the load of the catalyst is reduced, the temperature of a catalyst bed layer is maintained at 185 ℃ under the condition of 90% load, the hot spot temperature is reduced by 5-10 ℃, the reduction of the hot spot temperature is beneficial to the use of the catalyst, and the length of a catalyst crystal is reduced; the front and back series of catalysts participate in the reaction, and the hot spot temperature of the front and back series of catalysts is kept stable. The utilization efficiency of the catalyst is increased, and the waste of the catalyst in the subsequent series is avoided.

Drawings

Fig. 1 is a schematic structural diagram of a device for increasing a hydrogen-ester ratio, and comprises a preheater 1, a preheater 2, a circulating gas heater 3, a filter 4, a gas-gas heat exchanger 5, a cooler 6, a condenser 7, a gas-liquid separator 8, a first high-efficiency spray head 9 and a second high-efficiency spray head.

Fig. 2 is a schematic structural diagram of a preheater and a recycle gas heater, wherein fig. 1 shows the preheater 2, the recycle gas heater 8, a first high-efficiency spray head 9 and a second high-efficiency spray head.

Fig. 3 is a schematic diagram of the internal structure of the filter, wherein 3, the filter 10 and the porcelain ball.

Fig. 4 is a view showing the internal structure of the gas-liquid separator, and in fig. 7, the gas-liquid separator 11 and the demister are shown.

Detailed Description