CN215288657U - Gasoline hydrogenation system - Google Patents
Gasoline hydrogenation system Download PDFInfo
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- CN215288657U CN215288657U CN202120525797.2U CN202120525797U CN215288657U CN 215288657 U CN215288657 U CN 215288657U CN 202120525797 U CN202120525797 U CN 202120525797U CN 215288657 U CN215288657 U CN 215288657U
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Abstract
The utility model discloses a gasoline hydrogenation system, it includes one section hydrogenation charge pump, one section reaction effluent/mixed feeding heat exchanger, one section hydrogenation ware, one section hydrogenation heating furnace, back refined reactor, newly-increased refined diesel oil one section hydrogenation reaction feeding heat exchanger, catalytic gasoline buffer tank adds the hydrogenation reaction charge pump in advance, refined diesel oil/add the hydrogenation reaction feeding heat exchanger in advance, add the hydrogenation reaction feeding/reaction product heat exchanger in advance, newly-increased back refined reactor effluent/add the hydrogenation reaction feeding heat exchanger in advance, add the hydrogenation reaction feeding heater in advance, add the hydrogenation ware in advance, refined diesel oil air cooler. The system solves the problem of high-temperature heat waste of the refined reactor product and the refined diesel oil after the heat source in the prior art, effectively ensures the safe operation of the heat exchanger, greatly saves the steam consumption of the pre-hydrogenation reaction feeding heater and the power consumption of the refined diesel oil air cooler, and reduces the running load of the refined diesel oil air cooler.
Description
Technical Field
The utility model relates to a petrochemical industry technical field, concretely relates to utilize gasoline hydrogenation system of energy step recycle.
Background
In recent years, the rapid economic development of China promotes the rapid increase of gasoline consumption, and the gasoline is the second largest gasoline consuming country second to the United states. The consumption of a large amount of gasoline brings serious air pollution problem, and the reduction of the sulfur content in the gasoline is one of effective means for reducing the pollution. At present, the most widely applied technology is various gasoline selective hydrogenation technologies. In the prior art, a high-temperature heat source directly exchanges heat with mixed feeding of a shell pass of a heat exchanger at an initial temperature, the temperature difference is about 160 ℃, gradient utilization of high-temperature heat is not facilitated, waste of the high-temperature heat source is caused, meanwhile, the safety operation of the heat exchanger is influenced due to overlarge temperature difference, and the integral economic benefit of the whole plant is influenced by the uncoordinated phenomenon of energy utilization.
SUMMERY OF THE UTILITY MODEL
In order to solve the problem, the utility model provides a gasoline hydrogenation system which utilizes the process of energy step recycling.
In order to achieve the above object, the utility model adopts the following technical scheme:
a gasoline hydrogenation system comprises a catalytic gasoline buffer tank and a first-stage hydrogenation feed pump, wherein the catalytic gasoline buffer tank is connected with a pre-hydrogenation reaction feed pump, the pre-hydrogenation reaction feed pump enables products of the catalytic gasoline buffer tank to sequentially pass through a refined diesel oil/pre-hydrogenation reaction feed heat exchanger, a pre-hydrogenation reaction feed/reaction product heat exchanger, an effluent/pre-hydrogenation reaction feed heat exchanger of a newly-added post-refining reactor, the products are sent into a pre-hydrogenation reactor for reaction after heat exchange, and the products after reaction are discharged to a pre-fractionating tower after heat exchange through the pre-hydrogenation reaction feed/reaction product heat exchanger;
the first-stage hydrogenation feed pump sequentially passes materials through a newly-added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger, a first-stage reaction effluent/mixed feed heat exchanger and a first-stage reaction effluent/mixed feed heat exchanger, the materials are sent into a first-stage hydrogenation reactor to undergo first-stage hydrogenation reaction after heat exchange, the reacted products enter a post-refining reactor to react after being heated by a first-stage hydrogenation heating furnace, the reacted products pass through the first-stage reaction effluent/mixed feed heat exchanger, and the first-stage reaction effluent/mixed feed heat exchanger exchanges heat and then is sent into the newly-added post-refining reactor effluent/pre-hydrogenation reaction feed heat exchanger;
the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger is connected with a refined diesel oil conveying pipeline, the refined diesel oil conveying pipeline exchanges heat through the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger and the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger, and the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger is also connected with a refined diesel oil air cooler.
Two valves are arranged on a pipeline between the first-stage hydrogenation feed pump and the newly-added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger, a parallel pipeline a is arranged on a pipeline between the two valves, and the parallel pipeline a is communicated between the first-stage reaction effluent/mixed feed heat exchanger and a pipeline of the first-stage reaction effluent/mixed feed heat exchanger; a parallel pipeline d is also arranged between the first-stage reaction effluent/mixed feed heat exchanger and the first-stage reaction effluent/mixed feed heat exchanger, the parallel pipeline a and the parallel pipeline d are a first-stage hydrogenation reaction feed conveying pipeline, and a valve is arranged on the parallel pipeline a.
The pipeline of the pre-hydrogenation reaction feeding pump communicated with the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger is provided with a valve, the pipeline is provided with a parallel pipeline b and a parallel pipeline c after passing through the valve, the parallel pipeline b is communicated between the pre-hydrogenation reaction feeding/reaction product heat exchanger and the pipeline of the newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger, the parallel pipeline b is a circulating hydrogen conveying pipeline, the parallel pipeline b is provided with a valve, the parallel pipeline c is a hydrogen conveying pipeline, and the parallel pipeline c is provided with a valve.
The refined diesel oil conveying pipeline is provided with a valve, parallel pipelines e are arranged at the front and the rear of a newly-added refined diesel oil/first-section hydrogenation reaction feeding heat exchanger passing behind the valve, and the parallel pipelines e are refined diesel oil conveying pipelines.
The newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger and the newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger are U-shaped tubular heat exchangers.
The refined diesel oil conveying pipeline, the hydrogen conveying pipeline, the first-section hydrogenation reaction feeding conveying pipeline and the pre-hydrogenation reaction feeding conveying pipeline are all made of carbon steel.
The post-refining reactor, the pre-hydrogenation reactor and the first-stage hydrogenation reactor are made of alloy steel. Use the utility model discloses a beneficial effect is: the system solves the problem of high-temperature heat waste of the refined reactor product and the refined diesel oil after the heat source in the prior art, effectively ensures the safe operation of the heat exchanger, greatly saves the steam consumption of the pre-hydrogenation reaction feeding heater and the power consumption of the refined diesel oil air cooler, and reduces the running load of the refined diesel oil air cooler. Effectively improves the comprehensive economic benefit of the device and realizes the effective cascade utilization of the high-temperature heat of the post-refining reactor product and the refined diesel oil.
Drawings
Fig. 1 is a flow chart of the system of the present invention.
The reference numerals include: 9 is a first-stage hydrogenation feeding pump, 10 and 11 are first-stage reaction effluent/mixed feeding heat exchangers, 12 is a first-stage hydrogenation reactor, 13 is a first-stage hydrogenation heating furnace, 14 is a post-refining reactor, 15 is a newly-added refined diesel/first-stage hydrogenation reaction feeding heat exchanger, 16 is a catalytic gasoline buffer tank, 17 is a pre-hydrogenation reaction feeding pump, 18 is a refined diesel/pre-hydrogenation reaction feeding heat exchanger, 19 is a pre-hydrogenation reaction feeding/reaction product heat exchanger, 20 is a newly-added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger, 21 is a pre-hydrogenation reaction feeding heater, 22 is a pre-hydrogenation reactor, 23 is a refined diesel air cooler, 45 is a circulating hydrogen conveying pipeline, 46 is a hydrogen conveying pipeline, 47 is a refined diesel conveying pipeline, and 27 and 30 are first-stage hydrogenation reaction feeding conveying pipelines.
Detailed Description
In order to make the purpose, technical solution and advantages of the present technical solution more clear, the present technical solution is further described in detail below with reference to specific embodiments. It should be understood that the description is intended to be exemplary only, and is not intended to limit the scope of the present teachings.
The utility model discloses a gasoline hydrogenation system, it includes catalytic gasoline surge tank 16, one section hydrogenation charge pump 9, catalytic gasoline surge tank 16 is connected with and adds the hydrogenation charge pump 17 in advance, add hydrogenation charge pump 17 and loop through refined diesel oil with the product of catalytic gasoline surge tank 16/add hydrogenation reaction feed heat exchanger 18 in advance, add hydrogenation reaction feed/reaction product heat exchanger 19 in advance, add back refined reactor effluent/add hydrogenation reaction feed heat exchanger 20 in advance, send into after the heat transfer and add hydrogenation reaction 22 reaction, the product after the reaction is discharged to the prefractionator after the heat transfer of pre-hydrogenation reaction feed/reaction product heat exchanger 19;
the first-stage hydrogenation feed pump 9 sequentially passes the materials through a newly-added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger 15, a first-stage reaction effluent/mixed feed heat exchanger 10 and a first-stage reaction effluent/mixed feed heat exchanger 11, the materials are sent into a first-stage hydrogenation reactor 12 to undergo first-stage hydrogenation reaction after heat exchange, the reacted products enter a post-refining reactor 14 to react after being heated by a first-stage hydrogenation heating furnace 13, the reacted products pass through the first-stage reaction effluent/mixed feed heat exchanger 11, and the reacted products are sent into a newly-added post-refining reactor effluent/pre-hydrogenation reaction feed heat exchanger 20 after heat exchange by the first-stage reaction effluent/mixed feed heat exchanger 10;
the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger 15 is connected with a refined diesel oil conveying pipeline, the refined diesel oil conveying pipeline exchanges heat through the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger 15 and the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger 18, and the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger 18 is also connected with a refined diesel oil air cooler 23.
Two valves are arranged on a pipeline between the first-stage hydrogenation feed pump 9 and the newly-added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger 15, a parallel pipeline a30 is arranged on a pipeline between the two valves, and the parallel pipeline a30 is communicated between the pipelines of the first-stage reaction effluent/mixed feed heat exchanger 10 and the first-stage reaction effluent/mixed feed heat exchanger 11; a parallel pipeline d27 is also arranged between the first-stage reaction effluent/mixed feed heat exchanger 10 and the first-stage reaction effluent/mixed feed heat exchanger 11, a parallel pipeline a30 and a parallel pipeline d27 are first-stage hydrogenation reaction feed conveying pipelines, and a valve is arranged on the parallel pipeline a 30.
The pipeline of the pre-hydrogenation reaction feeding pump 17 communicated with the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger 18 is provided with a valve, the pipeline is provided with a parallel pipeline b45 and a parallel pipeline c46 after passing through the valve, the parallel pipeline b45 is communicated between the pre-hydrogenation reaction feeding/reaction product heat exchanger 19 and the pipeline of the newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger 20, the parallel pipeline b45 is a circulating hydrogen conveying pipeline, the parallel pipeline b45 is provided with a valve, the parallel pipeline c46 is a hydrogen conveying pipeline, and the parallel pipeline c46 is provided with a valve.
A valve is arranged on the refined diesel oil conveying pipeline, a parallel pipeline e47 is arranged at the front and the rear positions of the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger 15 passing behind the valve, and the parallel pipeline e47 is a refined diesel oil conveying pipeline.
The newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger 15 and the newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger 20 are U-shaped tubular heat exchangers.
The refined diesel oil conveying pipeline, the hydrogen conveying pipeline, the first-section hydrogenation reaction feeding conveying pipeline and the pre-hydrogenation reaction feeding conveying pipeline are all made of carbon steel.
The post-refining reactor 14, the pre-hydrogenation reactor 22 and the first hydrogenation reactor 12 are made of alloy steel.
The system has the following working procedures: the catalytic gasoline enters a catalytic gasoline buffer tank 16 for sedimentation and dehydration; the dehydrated raw oil enters a pre-hydrogenation reaction feeding pump 17 to be pressurized to about 2.4MPa, is mixed with a small amount of new hydrogen from the outside of a device boundary area, then is subjected to heat exchange with a refined diesel oil/pre-hydrogenation reaction feeding heat exchanger 18, a pre-hydrogenation reaction feeding/reaction product heat exchanger 19 and a newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger 20 in sequence, is increased to over 140 ℃ by a pre-hydrogenation reaction feeding heater 21 and then is fed into a pre-hydrogenation reactor 22, and reactions such as diene saturation, low molecular mercaptan sulfur conversion and the like are carried out under the conditions of lower reaction temperature and hydrogen-oil ratio. The reaction product is sent to a prefractionator to be divided into light gasoline and heavy gasoline after heat exchange.
The first-stage hydrogenation mixed feed is mixed with new hydrogen from the outside of the device and the supercharged circulating hydrogen, and the mixture is subjected to heat exchange through a newly added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger 15 and first-stage reaction effluent/mixed feed heat exchangers 11 and 10 to reach the required inlet temperature of a first-stage hydrogenation reactor 12, and then enters the first-stage hydrogenation reactor in a gas phase state. The first-stage hydrogenation reaction product is heated by a first-stage heating furnace 13 and then enters a post-refining reactor 14, and the reaction product of the post-refining reactor 14 is subjected to heat exchange by a first-stage reaction effluent/mixed feed heat exchanger 11 and a first-stage reaction effluent/mixed feed heat exchanger 10 and then is sent to a newly added post-refining reactor effluent/pre-hydrogenation reaction feed heat exchanger 20 for heat exchange.
In the system, the starting end of a refined diesel oil conveying pipeline is connected with a tube pass outlet of a refined diesel oil/raw oil heat exchanger of a diesel oil upgrading device, and the starting end of a circulating hydrogen conveying pipeline is connected with a circulating hydrogen compressor and then reaches a section of hydrogenation reaction feeding conveying pipeline; the starting end of the hydrogen conveying pipeline is from a hydrogen pipe network outside the device to a pre-hydrogenation reaction feeding conveying pipeline; the initial end of a hydrogenation reaction feeding conveying pipeline is linked with the bottom of the medium gasoline cutting tower and the extracted oil condenser, and the initial end of the pre-hydrogenation reaction feeding conveying pipeline is arranged outside the device.
In the embodiment, the gasoline hydrogenation process device of the refinery can save 27057.77 tons of steam each year, can save 315200 million electric quantities, has 705 ten million yuan of economic benefit each year and 1.2 months of investment recovery period.
Compared with the prior art, the system has the following beneficial effects:
1. by considering the principle of being nearby, the diesel oil upgrading devices which are adjacently arranged also have the condition of high-temperature heat source waste, and the high-temperature heat source is directly cooled to the normal temperature from about 200 ℃, so that enough heat can be supplemented. Therefore, the gasoline hydrogenation device and the diesel oil modification device are thermally combined, and after the thermal combination, the fuel and power consumption of the existing device are greatly saved, the cooling load of subsequent equipment is reduced, the comprehensive economic benefit is effectively improved, the problem of high-temperature heat source waste is solved, and the effective gradient utilization of the high-temperature heat source is realized.
2. The cascade utilization of the high-temperature heat source is successfully realized by utilizing a feasible design flow.
3. Reasonable layout and convenient control. In consideration of the principle of near, the high-temperature heat source of the diesel oil upgrading device which is adjacently arranged is reasonably utilized, the high-temperature heat source waste phenomenon of the diesel oil upgrading device and the gasoline hydrogenation device and the potential safety hazard of the devices are ingeniously solved, and the cascade utilization of energy optimization is successfully realized.
4. The equipment type selection and material are emphasized, and the method is safe and reliable.
The foregoing is only a preferred embodiment of the present invention, and many variations can be made in the specific embodiments and applications of the present invention by those skilled in the art without departing from the spirit of the present invention.
Claims (7)
1. A gasoline hydrogenation system comprises a catalytic gasoline buffer tank and a first-stage hydrogenation feed pump, and is characterized in that:
the catalytic gasoline buffer tank is connected with a pre-hydrogenation reaction feed pump, the pre-hydrogenation reaction feed pump sequentially passes the products of the catalytic gasoline buffer tank through a refined diesel oil/pre-hydrogenation reaction feed heat exchanger, a pre-hydrogenation reaction feed/reaction product heat exchanger, an effluent of a newly-added post-refining reactor/pre-hydrogenation reaction feed heat exchanger, the products are sent into the pre-hydrogenation reactor for reaction after heat exchange, and the products after reaction are discharged to a pre-fractionating tower after heat exchange through the pre-hydrogenation reaction feed/reaction product heat exchanger;
the first-stage hydrogenation feed pump sequentially passes materials through a newly-added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger, a first-stage reaction effluent/mixed feed heat exchanger and a first-stage reaction effluent/mixed feed heat exchanger, the materials are sent into a first-stage hydrogenation reactor to undergo first-stage hydrogenation reaction after heat exchange, the reacted products enter a post-refining reactor to react after being heated by a first-stage hydrogenation heating furnace, the reacted products pass through the first-stage reaction effluent/mixed feed heat exchanger, and the first-stage reaction effluent/mixed feed heat exchanger exchanges heat and then is sent into the newly-added post-refining reactor effluent/pre-hydrogenation reaction feed heat exchanger;
the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger is connected with a refined diesel oil conveying pipeline, the refined diesel oil conveying pipeline exchanges heat through the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger and the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger, and the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger is also connected with a refined diesel oil air cooler.
2. The gasoline hydrogenation system of claim 1, wherein:
two valves are arranged on a pipeline between the first-stage hydrogenation feed pump and the newly-added refined diesel oil/first-stage hydrogenation reaction feed heat exchanger, a parallel pipeline a is arranged on a pipeline between the two valves, and the parallel pipeline a is communicated between the first-stage reaction effluent/mixed feed heat exchanger and a pipeline of the first-stage reaction effluent/mixed feed heat exchanger; a parallel pipeline d is also arranged between the first-stage reaction effluent/mixed feed heat exchanger and the first-stage reaction effluent/mixed feed heat exchanger, the parallel pipeline a and the parallel pipeline d are a first-stage hydrogenation reaction feed conveying pipeline, and a valve is arranged on the parallel pipeline a.
3. The gasoline hydrogenation system of claim 1, wherein:
the pipeline of the pre-hydrogenation reaction feeding pump communicated with the refined diesel oil/pre-hydrogenation reaction feeding heat exchanger is provided with a valve, the pipeline is provided with a parallel pipeline b and a parallel pipeline c after passing through the valve, the parallel pipeline b is communicated between the pre-hydrogenation reaction feeding/reaction product heat exchanger and the pipeline of the newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger, the parallel pipeline b is a circulating hydrogen conveying pipeline, the parallel pipeline b is provided with a valve, the parallel pipeline c is a hydrogen conveying pipeline, and the parallel pipeline c is provided with a valve.
4. The gasoline hydrogenation system of claim 1, wherein:
the refined diesel oil conveying pipeline is provided with a valve, parallel pipelines e are arranged at the front and the rear of a newly-added refined diesel oil/first-section hydrogenation reaction feeding heat exchanger passing behind the valve, and the parallel pipelines e are refined diesel oil conveying pipelines.
5. The gasoline hydrogenation system of claim 1, wherein:
the newly added refined diesel oil/first-stage hydrogenation reaction feeding heat exchanger and the newly added refined reactor effluent/pre-hydrogenation reaction feeding heat exchanger are U-shaped tubular heat exchangers.
6. The gasoline hydrogenation system of claim 1, wherein:
the refined diesel oil conveying pipeline, the hydrogen conveying pipeline, the first-section hydrogenation reaction feeding conveying pipeline and the pre-hydrogenation reaction feeding conveying pipeline are all made of carbon steel.
7. The gasoline hydrogenation system of claim 1, wherein:
the post-refining reactor, the pre-hydrogenation reactor and the first-stage hydrogenation reactor are made of alloy steel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120525797.2U CN215288657U (en) | 2021-03-13 | 2021-03-13 | Gasoline hydrogenation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120525797.2U CN215288657U (en) | 2021-03-13 | 2021-03-13 | Gasoline hydrogenation system |
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| Publication Number | Publication Date |
|---|---|
| CN215288657U true CN215288657U (en) | 2021-12-24 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120525797.2U Expired - Fee Related CN215288657U (en) | 2021-03-13 | 2021-03-13 | Gasoline hydrogenation system |
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| CN (1) | CN215288657U (en) |
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2021
- 2021-03-13 CN CN202120525797.2U patent/CN215288657U/en not_active Expired - Fee Related
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Granted publication date: 20211224 |