CN214032356U - Energy-saving sulfur-tolerant shift system - Google Patents
Energy-saving sulfur-tolerant shift system Download PDFInfo
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- CN214032356U CN214032356U CN202022824450.6U CN202022824450U CN214032356U CN 214032356 U CN214032356 U CN 214032356U CN 202022824450 U CN202022824450 U CN 202022824450U CN 214032356 U CN214032356 U CN 214032356U
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Abstract
The utility model belongs to the technical field of synthetic ammonia production process, in particular to an energy-saving sulfur-tolerant shift system, which comprises a crude gas shift system and a shift gas cooling system, wherein a medium temperature shift furnace and a heat-insulating shift furnace are matched and used in parallel in a shift process flow to recover high-grade steam; a process gas route is optimized among the multi-stage conversion furnaces, and the system resistance is reduced; the energy recovery mode of the system is optimized, the steam grade number is reduced, the steam addition amount is reduced through the whole-process optimization, and the comprehensive consumption is reduced.
Description
Technical Field
The utility model belongs to the technical field of synthetic ammonia production process, especially, relate to an energy-conserving sulphur resistant transform system.
Background
The CO transformation is an important process in the production process of synthetic ammonia. The conversion device matched with high water-gas ratio and high CO water gas such as pulverized coal pressure gasification, coal water slurry pressure gasification, natural gas conversion and the like is required to complete the conversion task of CO and also consider the recovery task of heat brought into the conversion system by the previous process, particularly along with the progress of a nitrogen fertilizer production process and the popularization and application of a novel coal gasification technology in recent years, a continuous gasification technology is unprecedentedly developed, the content of CO in conversion gas is continuously improved on the basis of 30 percent of the traditional CO, some of the CO is even 70 to 85 percent, if the concentration of CO is more than 65 percent, the traditional CO conversion reaction is very violent, the conversion difficulty is extremely high, the reaction temperature is difficult to control, and the conversion of high water-gas ratio and high carbon monoxide in domestic operation at present basically adopts a cobalt-molybdenum catalyst wide temperature conversion process. Because the CO concentration is high and the water-gas ratio is high, if the dosage of the catalyst of the first shift converter is increased in the production process, the catalyst of the first shift converter is burnt off carelessly; the catalyst consumption of the first shift converter is reduced, the problem of overtemperature is solved, but the service life of the catalyst is short, the catalyst needs to be replaced once a year, the operation period of the catalyst is short, and the catalyst is not suitable for the requirement of a large-scale device; at present, the conversion of the pressurized gasification water gas is mostly four-stage heat insulation, a first conversion furnace is divided into two stages to be connected in parallel for air inlet, the number of system static equipment is 24, wherein 10 heat exchange equipment are provided, the process route is long, the system resistance reaches more than 0.6MPa, the heat energy recovery comprises saturated steam of 0.5MPa, 1.5MPa and 2.5MPa and hot water of 100 ℃, 180 ℃ and 220 ℃, and the consumption of cooling water per ton of ammonia is as high as 7800 Kg. The system has more low-grade heat energy and high operation energy consumption.
Although the CO concentration of the conversion process of the coal water slurry gasification is lower, the adopted conversion technology is still a process flow of three-section or four-section adiabatic reaction, sensible heat and latent heat recovery of each stage of water gas or converted gas needs a single indirect heat exchange device, the conversion processes of the shell and the space furnace powder gasification process have the same problems as the coal water slurry conversion, and are all the defects of long process route, large engineering investment, large system resistance, high low-grade heat energy, high energy consumption and the like.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing an energy-saving sulfur-tolerant shift system, which is characterized in that a medium temperature shift furnace and a heat-insulating shift furnace are matched and used in parallel in a shift process flow to recover high-grade steam; a process gas route is optimized among the multi-stage conversion furnaces, and the system resistance is reduced; the energy recovery mode of the system is optimized, and the steam grade number is reduced. The whole process is optimized to reduce the steam addition amount and reduce the comprehensive consumption.
In order to achieve the above purpose, the utility model adopts the technical scheme that:
an energy-saving sulfur-tolerant shift system comprises a first gas-liquid separator for separating crude gas from a gasification section, a shift converter feeding heat exchanger connected with the first gas-liquid separator, wherein gas coming out of the shift converter feeding heat exchanger is divided into two paths and respectively enters a first detoxification tank and a second detoxification tank, gas coming out of the first detoxification tank and the second detoxification tank is divided into two paths, one path of gas coming out of the first detoxification tank enters a first shift converter, one path of gas coming out of the second detoxification tank enters a second shift converter, gas coming out of the first shift converter and the second shift converter is converged and then enters a shift converter feeding gas heat exchanger tube pass, the other path of gas coming out of the first detoxification tank and the second detoxification tank enters a third shift converter, gas coming out of an outlet of the third shift converter and gas coming out of the shift converter feeding gas heat exchanger tube pass are converged and enter a first medium-pressure evaporation condenser, the outlet of the first medium-pressure evaporative condenser is connected with the inlet of a fourth shift converter, the gas from the fourth shift converter is contacted with the sprayed boiler water for heat exchange, then the unvaporized water is separated by a water spray purifier and discharged, the separated gas enters a second medium-pressure evaporative condenser and then is cooled by a condensate heater and then enters a fifth shift converter, the gas from the fifth shift converter enters a first low-pressure evaporative condenser for cooling and then enters a sixth shift converter, the shifted gas from the sixth shift converter is processed by a cooling system, the third, fourth and fifth shift converters are firstly integrated for process balance, the gas entering the third shift converter is communicated with the inlets of the fourth shift converter and the fifth shift converter, the load distribution of each stage of shift converter can be adjusted according to the gas components, the CO content index at the outlet is controlled, and in addition, the system resistance is effectively reduced by pipelines, the comprehensive energy consumption of the system is reduced, and the energy-saving effect is good.
Further, the cooling system comprises a boiler feed water preheater and a second low-pressure evaporative condenser connected with an outlet of the boiler feed water preheater, an outlet of the second low-pressure evaporative condenser is connected with a third low-pressure evaporative condenser, the converted gas from an outlet of the third low-pressure evaporative condenser enters a second gas-liquid separator to separate out steam condensate, and the converted gas enters a condensate preheater to be cooled and then enters a first conversion gas-water cooler tube pass to exchange heat and then enters a second conversion gas-water cooler tube pass and then enters a third gas-liquid separator to separate out condensate in the converter.
Furthermore, the shift converter feeding heat exchanger is provided with a tube pass and a shell pass, and gas discharged from the first gas-liquid separator enters the shift converter feeding heat exchanger shell pass and gas from the first shift converter in the tube pass for heat exchange.
Further, first transform stove, second transform stove, fourth transform stove, fifth transform stove and sixth transform stove are adiabatic transform stove, and the third transform stove is isothermal transform stove, the utility model discloses the parallelly connected use of isothermal transform stove and adiabatic transform stove collocation in the transform process flow retrieves high-grade steam, optimizes the process gas route between the multi-stage transform stove, reduces the system resistance, optimizes system energy recovery mode, reduces the progression such as steam. The whole process is optimized to reduce the steam addition amount and reduce the comprehensive consumption.
A conversion process of an energy-saving sulfur-tolerant conversion system comprises the following steps:
(1) crude gas shift reaction: raw gas from a gasification section at 3.718MPa and 211 ℃ enters a first gas-liquid separator through a valve, condensate in the raw gas is separated, the raw gas enters a shell pass of a charging gas heat exchanger of a shift converter, then the raw gas is divided into two paths and is respectively subjected to impurity removal in the gas through a first detoxification tank and a second detoxification tank, the gas from the first detoxification tank and the gas from the second detoxification tank are respectively divided into two paths, one path of gas from the first detoxification tank enters a first shift converter, one path of gas from the second detoxification tank enters a second shift converter, the gas from the first shift converter and the gas from the second shift converter are converged and then enter a tube pass of the charging gas heat exchanger of the shift converter, the raw gas is heated to 260 ℃, the raw gas is reduced to 311 ℃ per se, the other path of raw gas from the first detoxification tank and the second detoxification tank enters a third shift converter for isothermal conversion, the CO content is maintained at 290 ℃, the gas from the outlet of the third shift converter and the gas in the tube pass of the charging gas heat exchanger of the shift converter are converged and enter a first medium-pressure evaporation condenser for heat exchange, and then heat exchange are obtained When the temperature reaches 240 ℃ and 1.5MPa saturated steam, the saturated steam enters a fourth shift converter to react to 434 ℃, and the CO content is 6.7 percent, the saturated steam is sprayed into boiler water to be reduced to 338 ℃, then the saturated steam is sprayed into a water spray purifier to separate unvaporized water, the separated gas is reduced to 274 ℃ and 2.5MPa steam through a second medium-pressure evaporation condenser, the temperature is reduced to 220 ℃ through a condensate heater, the saturated steam enters a fifth shift converter to react to 260 ℃, the CO content is reduced to 1.0 percent, the gas discharged from the fifth shift converter enters a first low-pressure evaporation condenser to be reduced in temperature, and the gas enters a sixth shift converter through the low-pressure steam of 0.5MPa, until the CO conversion gas at the outlet of the shift converter is lower than 0.4 percent and the temperature is 204 ℃, and then the shift reaction of the raw gas is completed;
(2) and (3) changing gas and cooling treatment: cooling the shift gas from the step (1) to 181 ℃ through a boiler feed water preheater, then passing through a second low-pressure evaporative condenser and a third low-pressure evaporative condenser which are connected in parallel to produce a byproduct of saturated steam with the temperature of 0.3MPa and the temperature of 145 ℃, separating steam condensate from the shift gas in a second separator, passing the shift gas into a condensate preheater to cool to 84 ℃, passing the shift gas into a first shift gas water cooler tube pass to cool to 40 ℃, passing the shift gas into a second shift gas water cooler tube pass to cool to 24 ℃, finally passing through a third gas-liquid separator to separate condensate in the shift gas, namely cooling the shift gas, and sending the shift gas to a low-temperature methanol washing section.
The utility model has the advantages that:
1. the utility model discloses moderate temperature shift furnace and adiabatic shift furnace collocation use in parallel in the transform process flow, retrieve high-grade steam, optimize the process gas route between the multi-stage shift furnace, reduce system resistance, optimize system energy recuperation mode, reduce steam grade number, the full process is optimized and is reduced steam supplementary amount, reduces comprehensive consumption;
2. the third, fourth and fifth shift converters are integrated for process balance for the first time, the coal gas entering the third shift converter is communicated with inlets of the fourth shift converter and the fifth shift converter, the load distribution of each shift converter can be adjusted according to gas components, the CO content index of an outlet is controlled, in addition, a pipeline is directly connected, the system resistance is effectively reduced, the comprehensive energy consumption of the system is reduced, and the energy-saving effect is good;
3. according to the change of an energy recovery mode, the problems of high steam recovery grade and low grade are solved, and the steam recovery grade of a new process flow is mainly concentrated at 2.5Mpa and 0.3 Mpa;
4. an improved direction is explored for a chemical process reactor with large heat effect by using an isothermal converter in the energy-saving type conversion process technology, the basis of expanded production energy-saving reconstruction similar to a synthetic ammonia device and CO conversion process optimization and improvement of a methane conversion device in an oil-to-coal and gas-to-coal device is provided, the energy-saving type conversion process is not only suitable for a new synthetic ammonia device, but also can be used for reconstructing a conversion device which is put into operation and has high energy consumption, the technical equipment problem which is troubled for enterprises for a long time is solved, the energy-saving type conversion process can thoroughly eliminate the bottleneck restricting the high-load production and operation of the device, and also brings obvious economic benefits and social benefits for the enterprises, and the steam prices of 80 yuan/t, 120 yuan/t and 150 yuan/t according to 0.5MPa, 1.5MPa and 2.5MPa are respectively 850 yuan/t and 0.45 yuan/kWh, 0.8 yuan/t, and calculating the heating desalted water, the process condensate water of the deoxygenated water, the consumed cooling water and the like according to the coal consumption of 23 MJ converted from heat energy. Compared with the traditional conversion process, the energy-saving conversion process can save 142 yuan of operating cost per ton of ammonia, and 8520 ten thousand yuan per year for a single set of 600 kt/a ammonia synthesis device.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Detailed Description
As shown in the figure, crude gas from a gasification section at 3.718MPa and 211 ℃ enters a first gas-liquid separator 1 through a valve, condensate in the crude gas is separated, the crude gas enters a shell pass of a shift converter feeding heat exchanger 2, then impurities in the gas are removed through a first detoxification groove 3 and a second detoxification groove 4 in two paths, the gas from the first detoxification groove 3 and the second detoxification groove 4 is divided into two paths, one path of gas from the first detoxification groove 3 enters a first shift converter 5, one path of gas from the second detoxification groove 4 enters a second shift converter 6, the gas from the first shift converter 5 and the second shift converter 6 is converged and then enters a shift converter feeding gas heat exchanger 2 pipe pass, the crude gas is heated to 260 ℃, the crude gas is reduced to 311 ℃ per se, the other path of crude gas from the first detoxification groove 3 and the second detoxification groove 4 enters a third converter 7 for isothermal shift conversion, the isothermal temperature is maintained at 290 ℃, the CO content is 35 percent, the gas at the outlet of the third shift converter 7 and the gas at the tube pass of the shift converter feeding gas heat exchanger 2 are converged and enter a first medium-pressure evaporation condenser 8 for heat exchange to obtain saturated steam with the temperature of 240 ℃ and 1.5MPa, then the saturated steam enters a fourth shift converter 9 for reaction to reach the temperature of 434 ℃, the CO content is 6.7 percent, the saturated steam is sprayed into boiler water for cooling to 338 ℃, then the saturated steam is sprayed into a water spray purifier 10 for separating unvaporized water, the separated gas is cooled to 274 ℃ through a second medium-pressure evaporation condenser 11, the steam with the pressure of 2.5MPa is cooled to 220 ℃ through a condensate heater 12, the gas enters a fifth shift converter 13 for reaction to reach the temperature of 260 ℃ and the CO content is reduced to 1.0 percent, the gas from the fifth shift converter 13 enters a first low-pressure evaporation condenser 14 for cooling, and enters a sixth shift converter 15 through low-pressure steam with the pressure of 0.5MPa, the shift converter outlet, the CO is changed to reach the temperature of 204, the conversion gas is cooled to 181 ℃ by a boiler feed water preheater 16, then passes through a second low-pressure evaporative condenser 17 and a third low-pressure evaporative condenser 18 which are connected in parallel to produce a byproduct of saturated steam with the temperature of 0.3MPa and the temperature of 145 ℃, enters a second gas-liquid separator 19 to separate steam condensate, enters a condensate preheater 20 to cool to 84 ℃, enters a first conversion gas water cooler 21 tube pass to cool to 40 ℃, enters a second conversion gas water cooler 22 tube pass to cool to 24 ℃, finally passes through a third gas-liquid separator 23 to separate condensate in the conversion gas, namely the conversion gas is cooled, the conversion gas is sent to a low-temperature methanol washing section, the first conversion furnace 5, the second conversion furnace 6, the fourth conversion furnace 9, the fifth conversion furnace 13 and the sixth conversion furnace 15 are heat-insulation conversion furnaces, the third conversion furnace 7 is an isothermal conversion furnace, the isothermal conversion furnace and the adiabatic conversion furnace are used in parallel in the conversion process flow, high-grade steam is recycled, a process gas route is optimized among the multi-stage conversion furnaces, system resistance is reduced, a system energy recovery mode is optimized, the number of steam stages is reduced, the steam addition amount is reduced through full-process optimization, and comprehensive consumption is reduced.
Comparative experiment
At present, the conversion of pressurized gasification water gas is mostly four-section heat insulation, a first conversion furnace is divided into two sections to be connected in parallel for air inlet, 24 static devices of a system are provided, wherein 10 heat exchange devices are provided, the process route is long, the system resistance reaches over 0.6MPa, the heat energy recovery comprises saturated steam of 0.5MPa, 1.5MPa and 2.5MPa and hot water of 100 ℃, 180 ℃ and 220 ℃, the consumption of cooling water per ton of ammonia is as high as 7800Kg, the system has more low-grade heat energy, and the operation energy consumption is high. Although the CO concentration of the transformation process of the coal water slurry gasification is lower, the adopted transformation technology is still a process flow of three-stage or four-stage adiabatic reaction; the isothermal conversion furnace is used for exploring an improvement direction for a chemical process reactor with large heat effect in the energy-saving conversion process technology, and the basis for expanding production, saving energy and improving the yield of a similar synthetic ammonia device and optimizing and improving the CO conversion process of a methane conversion device in an oil-to-coal and gas-to-coal device is provided, so that the isothermal conversion furnace is not only suitable for a new synthetic ammonia device, but also can be used for improving a conversion device which is put into operation and has high energy consumption, and the technical equipment problem which troubles enterprises for a long time is solved. The energy-saving transformation process not only can thoroughly eliminate the bottleneck restricting the high-load production and operation of the device, but also brings obvious economic and social benefits to enterprises.
According to the steam prices of 0.5MPa, 1.5MPa and 2.5MPa of 80 yuan/t, 120 yuan/t and 150 yuan/t and the coal, electricity prices, circulating water and the like of raw materials of 850 yuan/t, 0.45 yuan/kWh and 0.8 yuan/t, the heating desalted water, the process condensate water of the deoxygenated water, the consumed cooling water and the like are all calculated according to the coal consumption of 23 MJ converted from heat energy.
Claims (3)
1. An energy-saving sulfur tolerant shift system, characterized by: the system comprises a first gas-liquid separator for separating crude gas from a gasification section, and a shift converter feeding heat exchanger connected with the first gas-liquid separator, wherein gas coming out of the shift converter feeding heat exchanger is divided into two paths and respectively enters a first detoxification tank and a second detoxification tank, gas coming out of the first detoxification tank and the second detoxification tank is respectively divided into two paths, one path of gas coming out of the first detoxification tank enters a first shift converter, one path of gas coming out of the second detoxification tank enters a second shift converter, gas coming out of the first shift converter and the second shift converter is converged and then enters a shift converter feeding gas heat exchanger tube pass, the other path of gas coming out of the first detoxification tank and the second shift converter enters a third shift converter, gas coming out of an outlet of the third shift converter and gas coming out of the shift converter feeding gas heat exchanger tube pass are converged and enter a first medium-pressure evaporative condenser, an outlet of the first medium-pressure evaporative condenser is connected with an inlet of a fourth shift converter, the gas from the fourth shift converter is contacted with the sprayed boiler water for heat exchange, then the unvaporized water is separated by the water spray purifier and discharged, the separated gas enters the second medium-pressure evaporation condenser and then is cooled by the condensate heater and then enters the fifth shift converter, the gas from the fifth shift converter enters the first low-pressure evaporation condenser for cooling and then enters the sixth shift converter, and the shift gas from the sixth shift converter is processed by the cooling system, wherein the first shift converter, the second shift converter, the fourth shift converter, the fifth shift converter and the sixth shift converter are adiabatic shift converters, and the third shift converter is an isothermal shift converter.
2. The energy efficient sulfur tolerant shift system of claim 1, wherein: the cooling system comprises a boiler feed water preheater and a second low-pressure evaporative condenser connected with an outlet of the boiler feed water preheater, an outlet of the second low-pressure evaporative condenser is connected with a third low-pressure evaporative condenser, the converted gas from an outlet of the third low-pressure evaporative condenser enters a second gas-liquid separator to separate out steam condensate, and the converted gas enters a condensate preheater for cooling and then enters a first conversion gas-water cooler tube pass for heat exchange and then enters a second conversion gas-water cooler tube pass and then enters a third gas-liquid separator to separate out condensate in the converter.
3. The energy efficient sulfur tolerant shift system according to claim 1 or 2, wherein: the shift converter feeding heat exchanger is provided with a tube pass and a shell pass, and gas discharged from the first gas-liquid separator enters the shell pass of the shift converter feeding heat exchanger and gas from the first shift converter in the tube pass for heat exchange.
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| CN202022824450.6U CN214032356U (en) | 2020-11-27 | 2020-11-27 | Energy-saving sulfur-tolerant shift system |
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| CN202022824450.6U CN214032356U (en) | 2020-11-27 | 2020-11-27 | Energy-saving sulfur-tolerant shift system |
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