CN112499583B - System optimization process and equipment capable of improving compression effect of synthesis gas compressor - Google Patents
System optimization process and equipment capable of improving compression effect of synthesis gas compressor Download PDFInfo
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- CN112499583B CN112499583B CN202011518872.9A CN202011518872A CN112499583B CN 112499583 B CN112499583 B CN 112499583B CN 202011518872 A CN202011518872 A CN 202011518872A CN 112499583 B CN112499583 B CN 112499583B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
- C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
- C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28G—CLEANING OF INTERNAL OR EXTERNAL SURFACES OF HEAT-EXCHANGE OR HEAT-TRANSFER CONDUITS, e.g. WATER TUBES OR BOILERS
- F28G1/00—Non-rotary, e.g. reciprocated, appliances
- F28G1/12—Fluid-propelled scrapers, bullets, or like solid bodies
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- 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
Abstract
The invention discloses a system optimization process capable of improving the compression effect of a synthesis gas compressor, which mainly comprises the following steps: s1, preparing raw material gas; s2, compressing the synthesis gas; s3, converting the synthetic gas into ammonia, connecting a water cooler at the outlet of the synthetic tower in parallel on the basis of the water cooler at the outlet of the original synthetic tower in the process step, and converting the existing combined NH3The condenser is changed into two identical NH3The condensers are connected in parallel, the rubber ball cleaning device is additionally arranged, and the two intermittent coolers are connected in parallel, so that the process can reduce the energy consumption of the unit and reduce the steam consumption of the unit under the condition of ensuring normal production, and the rubber ball cleaning device cleans the inner wall pipe of the heat exchange equipment, so that the influence of dirt resistance on the total heat transfer coefficient is reduced, the heat exchange efficiency is higher under the same energy consumption, and the process is suitable for wide popularization.
Description
Technical Field
The invention relates to the technical field of synthesis gas preparation, in particular to a system optimization process and equipment capable of improving the compression effect of a synthesis gas compressor.
Background
The KBR ammonia synthesis system is applied to a plurality of large chemical fertilizer production projects and obtains better effect. However, in the high temperature period in summer, the temperature of the circulating water entering the circulating water cooling tower is increased due to the rise of the environmental temperature, the temperature of the water leaving the circulating water cooling tower is further increased, the temperature of the circulating cooling water is continuously increased, the temperature of the circulating water is as high as 35 ℃, the heat exchange effect of the water cooler is further deteriorated, and vicious circle is generated. Therefore, under the same load, the temperature of liquid ammonia at the outlet of the ammonia cooler is continuously increased, the vacuum degree of the two units is also reduced, the rotating speed and the steam consumption of the two units are increased to some extent, and the production load is limited to a certain extent.
The production load is limited by the heat exchange capacity of the associated heat exchange equipment within the system. The load of the heat exchange equipment is related to the heat exchange area, the total heat transfer coefficient and the average temperature difference. For a certain heat exchange device, after long-term operation, a certain dirt layer can be formed on the pipe walls of the inner heat exchange pipe and the outer heat exchange pipe, so that the total heat transfer coefficient is greatly reduced, and the temperature of circulating water is increased by high temperature in summer, so that the average temperature difference is directly reduced.
Disclosure of Invention
In order to solve the technical problems, the invention provides a system optimization process and equipment for improving the compression effect of a synthesis gas compressor.
The technical points of the invention are as follows:
a system optimization process capable of improving the compression effect of a synthesis gas compressor mainly comprises the following steps:
s1 preparation of raw material gas
The synthesis gas comes from the boundary region, and is introduced into the separation tank of the synthesis gas compressor through a stop valve, and the pressure value of the outlet of the separation tank of the synthesis gas compressor is controlled as follows: 2500-3000Kpa, after the raw material gas passes through a separation tank of a synthesis gas compressor, the components are controlled in the following range according to the volume fraction ratio: h2：70-75％，N2: 20-25%, while: CO + CO2+O2≤1ppmv，Ar+CH4≤2ppmv；
S2, compressing synthetic gas
And (3) introducing the raw material gas in the S1 into a centrifugal compressor in the synthesis gas synthesis tower, wherein the centrifugal compressor is powered by a steam turbine, two surface coolers for different workload treatments are connected in parallel on the steam turbine, and the ratio of the charging amount of nitrogen to the charging amount of hydrogen through a bypass is as follows: 3-3.5:1, introducing synthesis gas into a centrifugal compressor, mixing a plurality of strands of gas in the centrifugal compressor, compressing the mixed gas to 14820-minus 15410Kpa at 50-60 ℃ before entering a synthesis loop, preheating the mixed gas in the tube pass of an inlet heat exchanger of an ammonia synthesis tower, raising the temperature of the gas to 200 ℃, introducing the gas into a cold gas bypass for controlling the inlet temperature of the heat exchanger on the tube pass of a gas inlet of the tower, controlling the bypass by a DCS (distributed control system) control valve, introducing the circulating gas into the centrifugal compressor at the temperature of 30 ℃ and the pressure of 14698Kpa, setting the gas flow at the inlet of a first section of the centrifugal compressor to be 60000-minus 65000kg/h, introducing the gas into the shell pass of two identical intermittent coolers connected in parallel, further reducing the shell temperature of the synthesis gas to 38 ℃ on the shell pass of the intermittent coolers, and introducing the synthesis gas into the inlet of a second stage of the centrifugal compressor after passing through a check valve and a hydraulic auxiliary check valve, the synthesis gas passing through the second-stage inlet flows to a circulating gas part of the centrifugal compressor from an inner outlet, and the circulating gas of the centrifugal compressor is cooled to 38 ℃ in two synthesis tower outlet water coolers connected in parallel at the synthesis tower outlet;
s3 conversion of syngas to ammonia
Introducing the synthesis gas leaving the synthesis gas synthesis tower into an ammonia synthesis tower, wherein the space velocity of the ammonia synthesis tower is set to 8500h-1Controlling the temperature of the synthesis gas of a heat exchanger tube pass at an inlet of an ammonia synthesis tower to be between 185-200 ℃, then introducing the gas into a first layer bed through a plurality of lines, communicating a tube pass outlet of a heat exchanger at an outlet of the synthesis tower with a gas start-up heating furnace for raising the temperature of a catalyst bed to a reaction temperature after parking, introducing the gas flow into the heat exchanger tube pass of the first catalyst layer bed, introducing the gas flow to the outlet gas of the first layer bed for heat exchange, introducing the gas to the top of the first layer bed and radially passing through the bed, introducing the gas flow out of the bottom of the bed and directly passing through a channel to the shell pass of the heat exchanger of the first catalyst layer bed, introducing cold gas of a cold shock line into the first layer bed instead of passing through an annular gap, directly injecting and mixing the cold gas flow with the gas flow before the gas flows into the shell pass of the heat exchanger of the first catalyst layer bed, further cooling the gas flow at the shell pass of the heat exchanger of the first catalyst layer bed to 76 ℃, and introducing the synthesis gas leaving the shell pass of the heat exchanger of the first catalyst layer bed from the outlet of the synthesis tower through a water cooling loop isolating valve at an outlet of the synthesis tower The outlet of the reactor flows out, the temperature of the synthetic gas is further reduced to 35 ℃, and the cooled synthetic gas enters NH3CondenserFurther cooled and condensed in NH3The condenser is externally connected with an NH3Separator, tower gas and from NH3The synthesis gas returned by the separator undergoes internal heat exchange and is cooled by the cold ammonia outside the tubes, causing liquid NH to form3Boiling at two different temperatures of 14.7 ℃ and-3.2 ℃ to form NH3A rubber ball cleaning device is arranged on the condenser, and prepared NH is adopted3Separating the synthesis gas in an ammonia separator to obtain the prepared NH3And (4) entering a flash evaporation tank, and freezing and purifying the ammonia condensed by the synthesis loop through a three-stage ammonia freezing system.
Further, in S3, the gas is introduced into the first bed by the following lines: the first one is: the gas flows from the annular space of the ammonia synthesis tower to the tube pass of the first catalyst bed heat exchanger and then flows to the first bed layer; a second bar: gas flows into the first bed through a plurality of quenching lines; and a third: the gas flows to the first layer bed through the second catalyst layer bed heat exchanger; fourth, the method comprises the following steps: the gas passes through the coils of the start-up heater to the first bed.
Further, the gas flow of the second catalyst layer bed heat exchanger is controlled to be less than 70000kg/h, and the pressure is controlled to be: 8-15Mpa, which prevents the other bypass inlet pressure from being too low when the gas flow is too large and the equipment is damaged.
Furthermore, the centrifugal compressor is composed of a fresh air compression part and an isolated circulating air compression impeller, raw material gases are mixed in the compressor, and the mixing effect of the fresh air in the compressor is better.
Furthermore, the second-stage inlet is provided with a filter for removing impurities, so that the impurities are prevented from blocking the outlet, and the synthesis loop cannot be circulated.
Further, the equipment used in the process comprises: a syngas compressor separator tank for preparing a feed gas, a syngas synthesis column for syngas compression, an ammonia synthesis column for converting syngas to ammonia, the syngas synthesis column comprising within: a centrifugal compressor for mixing the synthetic gas, a heat exchanger arranged at the inlet of the synthetic gas synthesis tower, a cold gas bypass communicated with the heat exchanger and used for controlling the inlet of the heat exchanger, a DCS control valve used for controlling the bypass, and a heat exchanger connected with the inlet of the synthetic gas synthesis towerHeart formula compressor intercommunication and two the same intermittent type coolers of parallel arrangement, set up at the converter exit and two converter exit water coolers of parallel arrangement, the entrance of ammonia converter also is provided with the heat exchanger, and ammonia converter is inside to include: NH (NH)3A condenser connected to the NH3A rubber ball cleaning device (1) on the condenser, which is externally connected with the NH3NH on condenser3Separator, the glueballs belt cleaning device includes: the heat exchange equipment comprises a plurality of rubber balls, a ball feeding device for cleaning the rubber balls, a ball inlet pipe, a ball outlet pipe and a circulating mechanism, wherein the ball inlet pipe and the ball outlet pipe are connected to the ball feeding device, and the circulating mechanism is used for circularly cleaning circulating water inside the rubber ball cleaning device.
Further, the ball feeding device includes: spherical net, setting are in send the inside ball runner, the setting of sending of net to be in send a plurality of deflectors on the ball runner, the inlet tube comprises multisection spiral pipe, and the diameter of every section spiral pipe to the direction of sending the net progressively decreases layer by layer, circulation mechanism includes: circulation room, setting are in circulation roller bearing in the circulation room, setting are used for communicateing rubber ball belt cleaning device's circulation feed liquor pipe on the circulation room, set up and be used for the intercommunication on the circulation room send the circulation drain pipe of net, all be carved with the washing line on every section spiral pipe, the circulation room extracts the circulating water through the circulating pump, and rubber ball belt cleaning device possesses the self-cleaning function that carries out self-cleaning function and circulating water to the rubber ball.
Compared with the prior art, the invention has the beneficial effects that:
first, existing NH3The condenser is longer, and the temperature difference between the inlet and the outlet is larger, so that the stress at the inlet and the outlet of the equipment is larger, namely NH3The heat exchange tube of the condenser is stressed greatly and is easy to cause inner leakage, and the invention uses two small NH3The condensers are connected in parallel, so that the stress of the heat exchange pipe is reduced, and the compressor is further reducedAnd (5) steam energy consumption.
Secondly, the circulating gas of the synthesis gas compressor is connected with two synthesis tower outlet water coolers in parallel at the outlet of the synthesis tower, a synthesis gas pipeline is led out from a main pipe of the synthesis tower outlet water cooler to be connected with the newly-added synthesis tower outlet water cooler, the synthesis gas is led out of a pipeline, the synthesis gas out of the synthesis tower outlet water cooler A is converged to a main pipe of the synthesis tower outlet water cooler, the circulating water pipeline of the synthesis tower outlet water cooler is connected with the circulating water pipeline of the synthesis tower outlet water cooler, and the temperature of the synthesis gas is further cooled.
Thirdly, in the prior heat exchange equipment, a certain dirt layer is formed on the pipe wall of the inner heat exchange pipe and the outer heat exchange pipe after long-term operation, so that the total heat transfer coefficient is greatly reduced, the temperature of circulating water is increased due to high temperature in summer, and the average temperature difference is directly reduced.
Drawings
FIG. 1 is a front view of a schematic structural view of a rubber ball cleaning device according to the present invention;
FIG. 2 is a front view of a schematic view of the inlet tube of the present invention.
The device comprises a rubber ball cleaning device 1, a rubber ball cleaning device 2, a ball feeding device 21, a ball feeding net 22, a ball feeding rotating wheel 23, a guide plate 3, a ball inlet pipe 31, a spiral pipe 311, cleaning lines 4, a ball outlet pipe 5, a rubber ball 6, a circulating mechanism 61, a circulating chamber 62, a circulating roller 621, an adsorption hole 63, a circulating liquid inlet pipe 64, a circulating liquid outlet pipe 7 and a circulating pump.
Detailed Description
The first embodiment is as follows:
a system optimization process capable of improving the compression effect of a synthesis gas compressor mainly comprises the following steps:
s1 preparation of raw material gas
The synthesis gas comes fromOutside the boundary region, synthetic gas compressor knockout drum is let in through a trip valve to the pressure value of control synthetic gas compressor knockout drum export is: 2500Kpa, after the raw material gas passes through a separation tank of a synthesis gas compressor, the components are controlled in the following range according to the volume fraction ratio: h2：75％，N2: 25%, and simultaneously: CO + CO2+O2＝0.8ppmv，Ar+CH4＝1.6ppmv；
S2, compressing synthetic gas
And (3) introducing the raw material gas in the S1 into a centrifugal compressor in the synthesis gas synthesis tower, wherein the centrifugal compressor is powered by a steam turbine, two surface coolers for different workload treatments are connected in parallel on the steam turbine, and the ratio of the charging amount of nitrogen to the charging amount of hydrogen through a bypass is as follows: 3.3:1 introducing synthetic gas into a centrifugal compressor, mixing a plurality of strands of gas in the centrifugal compressor, compressing the mixed gas to 14820Kpa at 55 ℃ before entering a synthesis loop, preheating the gas in a tube pass of an inlet heat exchanger of an ammonia synthesis tower to raise the temperature of the gas to 200 ℃, introducing the gas into a cold gas bypass for controlling the inlet temperature of the heat exchanger on a gas inlet tube pass of the tower, controlling the bypass by a DCS control valve, introducing the circulating gas into the centrifugal compressor at the temperature of 30 ℃ and the pressure of 14698Kpa, setting the gas flow at a first section inlet of the centrifugal compressor to be 60000kg/h, introducing the gas into shell passes of two identical intermittent coolers connected in parallel, further reducing the shell temperature of the synthetic gas to 38 ℃ on the shell pass of the intermittent coolers, introducing the synthetic gas into a second stage inlet of the centrifugal compressor after passing through a check valve and a hydraulic auxiliary check valve, and flowing the synthetic gas passing through the second stage inlet from an inner outlet to the circulating gas part of the centrifugal compressor, the circulating gas of the centrifugal compressor is cooled to 38 ℃ in two synthesis tower outlet water coolers connected in parallel at the outlet of the synthesis tower;
s3 conversion of syngas to ammonia
Introducing the synthesis gas leaving the synthesis gas synthesis tower into an ammonia synthesis tower, wherein the space velocity of the ammonia synthesis tower is set to 8500h-1Controlling the temperature of the synthesis gas at the tube side of a heat exchanger at the inlet of the ammonia synthesis tower to be 185 ℃, and then introducing the gas into the first layer of bed through a plurality of lines to synthesizeThe tube pass outlet of the tower outlet heat exchanger is communicated with a gas start-up heating furnace for raising the temperature of a catalyst bed layer to the reaction temperature after stopping, the gas flow enters the tube pass of the first catalyst layer bed heat exchanger, at the moment, the gas flow flows to the outlet gas of the first layer bed for heat exchange, the gas flows to the top of the first layer bed and radially passes through the bed layer, the gas flow flows out of the bottom of the bed and directly passes through a channel to the shell pass of the first catalyst layer bed heat exchanger, cold gas on a cold shock line does not pass through an annular space, but directly injected and mixed with the gas flow before flowing out of the first layer bed and entering the shell pass of the first catalyst layer bed heat exchanger, the gas flow at the outlet of the ammonia synthesis tower is further cooled to 76 ℃ in the shell pass of the first catalyst layer bed heat exchanger, and is separated from NH3The synthesis gas with the shell pass of the first catalyst bed heat exchanger flows out of the outlet of the water cooler at the outlet of the synthesis tower through a circulating loop isolating valve, the temperature of the synthesis gas is further reduced to 35 ℃, the cooled synthesis gas enters a condenser to be further cooled and condensed, and NH is generated3The condenser is externally connected with an NH3Separator, tower gas and from NH3The synthesis gas returned by the separator undergoes internal heat exchange and is cooled by the cold ammonia outside the tubes, causing liquid NH to form3Boiling at two different temperatures of 14.7 ℃ and-3.2 ℃ to form NH3A rubber ball cleaning device 1 is arranged on the condenser, and prepared NH is adopted3Separating the synthesis gas in an ammonia separator to obtain the prepared NH3And (4) entering a flash evaporation tank, and freezing and purifying the ammonia condensed by the synthesis loop through a three-stage ammonia freezing system.
The centrifugal compressor consists of a fresh gas compression section and an isolated recycle gas compression impeller, the feed gases being mixed inside the compressor.
The second stage inlet is fitted with a filter to remove impurities.
The equipment used in the process comprises: a syngas compressor separation tank for preparing a feed gas, a syngas synthesis column for syngas compression, an ammonia synthesis column for converting syngas to ammonia, the syngas synthesis column comprising therein: a centrifugal compressor for mixing the synthetic gas, a heat exchanger arranged at the inlet of the synthetic gas synthesis tower, a cold gas bypass communicated with the heat exchanger for controlling the inlet of the heat exchanger, a heat exchanger for mixing the synthetic gas and the cold gasThe DCS control valve of control bypass, with centrifugal compressor intercommunication and two the same intermittent cooling wares of parallel arrangement, set up at the converter exit and two converter exit water coolers of parallel arrangement, the entrance of ammonia converter also is provided with the heat exchanger, and ammonia converter inside includes: NH (NH)3A condenser connected to the NH3The rubber ball cleaning device 1 on the condenser is externally connected with the NH3NH on condenser3Separator, the rubber ball belt cleaning device 1 includes: the glue ball cleaning device comprises a plurality of glue balls 5, a ball feeding device 2 for cleaning the glue balls, a ball inlet pipe 3 and a ball outlet hall 4 which are connected to the ball feeding device 2, and a circulating mechanism 6 for circularly cleaning circulating water inside the glue ball cleaning device 1.
The ball feeding device 2 includes: spherical net 21 of sending, the setting is in send the inside ball runner 22 of sending of net 21, set up a plurality of deflectors 23 on the ball runner 22 of sending, the inlet tube 3 comprises multisection spiral pipe 31, and every section spiral pipe 31 the diameter to the direction layer upon layer of sending net 21 decrements, circulation mechanism 6 includes: the circulating device comprises a circulating chamber 61, a circulating roller 62 arranged in the circulating chamber 61, a circulating liquid inlet pipe 63 arranged on the circulating chamber 61 and used for communicating with the rubber ball cleaning device 1, and a circulating liquid outlet pipe 64 arranged on the circulating chamber 61 and used for communicating with the ball delivery net 21, wherein the circulating chamber 6 pumps circulating water through a circulating pump 7, and cleaning lines 311 are engraved on each section of spiral pipe 31.
Will enter bulb 3 and NH3One end of the outlet of the condenser is connected with a ball outlet chamber 4 and NH3One end of the inlet of the condenser is connected to enable the rubber ball 5 to be in NH state3The circulating pipe inner loop of condenser washs, and glueballs 5 are constantly extruded through spiral pipe 31 to accomplish surface cleaning and the extrusion of internal circulation water through washing line 311, transport to play bulb 4 after the rethread send ball device 2 to refill the water inflation with glueballs 5 after the extrusion, circulation mechanism 6 can circulate the washing liquid to sending in the ball device 2 and purify.
The use and data recording by one year time yields: the average value of the vacuum values in the syngas compressor is: 83kpa (g), average steam consumption of the compressor: 74.85 t/h.
Example two:
the difference from the first embodiment is that
S1 preparation of raw material gas
The synthesis gas comes from the boundary region, and is introduced into the separation tank of the synthesis gas compressor through a stop valve, and the pressure value of the outlet of the separation tank of the synthesis gas compressor is controlled as follows: 2800Kpa, after the raw material gas passes through a separation tank of a synthesis gas compressor, the volume fraction ratio of the components is controlled in the following range: h2：75％，N2: 25%, and simultaneously: CO + CO2+O2＝0.8ppmv，Ar+CH4＝1.6ppmv；
S2, compressing synthetic gas
And (3) introducing the raw material gas in the S1 into a centrifugal compressor in the synthesis gas synthesis tower, wherein the centrifugal compressor is powered by a steam turbine, two surface coolers for different workload treatments are connected in parallel on the steam turbine, and the ratio of the charging amount of nitrogen to the charging amount of hydrogen through a bypass is as follows: 3.3:1 introducing synthetic gas into a centrifugal compressor, mixing a plurality of strands of gas in the centrifugal compressor, compressing the mixed gas to 15410Kpa at 55 ℃ before entering a synthesis loop, preheating the gas in a tube pass of an inlet heat exchanger of an ammonia synthesis tower to increase the temperature of the gas to 200 ℃, introducing the gas into a cold gas bypass for controlling the inlet temperature of the heat exchanger on a gas-feeding tube pass of the tower, controlling the bypass by a DCS (distributed control system) control valve, introducing the circulating gas into the centrifugal compressor at the temperature of 30 ℃ and the pressure of 14698Kpa, setting the gas flow rate of a first-section inlet of the centrifugal compressor to be 63150kg/h, introducing the gas into shell passes of two identical intermittent coolers connected in parallel, further reducing the shell temperature of the synthetic gas to 38 ℃, introducing the synthetic gas into a second-stage inlet of the centrifugal compressor after passing through a check valve and a hydraulic auxiliary check valve, and flowing the synthetic gas passing through the second-stage inlet from an internal outlet to the circulating gas part of the centrifugal compressor, the recycle gas from the centrifugal compressor was cooled to 38 c in two synthesis column outlet water coolers in parallel at the synthesis column outlet.
The use and data recording by one year time yields: the average value of the vacuum values in the syngas compressor is: -84kpa (g), average steam consumption of the compressor: 74.62 t/h.
Example three:
the difference from the second embodiment is that
In S3, the gas is introduced into the first bed by the following lines: the first one is: the gas flows from the annular space of the ammonia synthesis tower to the tube pass of the first catalyst bed heat exchanger and then flows to the first bed layer; a second bar: gas flows into the first bed through a plurality of quenching lines; and a third: the gas flows to the first layer bed through the second catalyst layer bed heat exchanger; fourth, the method comprises the following steps: the gas passes through the coils of the start-up heater to the first bed.
The use and data recording by one year time yields: the average value of the vacuum values in the syngas compressor is: 83kpa (g), average steam consumption of the compressor: 74.58 t/h.
Example four:
the difference from the third embodiment is that
The gas flow rate of the second catalyst layer bed heat exchanger is controlled to be 4500kg/h, and the pressure is controlled to be: 13 MPa.
The use and data recording by one year time yields: the average value of the vacuum values in the syngas compressor is: 83kpa (g), average steam consumption of the compressor: 74.51 t/h.
Example five:
the difference from the fourth embodiment is that
Fifth example in S3, NH3The condenser is not provided with a rubber ball cleaning device.
The use and data recording by one year time yields: the average value of the vacuum values in the syngas compressor is: 81kPa (G), the average steam consumption of the compressor being: 75.93 t/h.
Example six:
the difference from the fifth embodiment is that
Sixth example described using a single NH3A condenser and a single synthesis column outlet water cooler.
The use and data recording by one year time yields: the average value of the vacuum values in the syngas compressor is: 83kpa (g), average steam consumption of the compressor: 74.85 t/h.
It can be known from the first to the fourth embodiments that the influence of the temperature of the synthesis gas and the pressure of the compressor on the process energy consumption is large, the energy consumption generated by the synthesis gas preparation process of the fourth embodiment is minimum, and the guaranteed true control value of the pressure of the compressor is also optimal3The condenser combination and the water cooler combination at the outlet of the synthesis tower can more effectively reduce the temperature of synthesis gas and circulating water and ensure that the steam consumption is the lowest.
Claims (5)
1. A system optimization process capable of improving the compression effect of a synthesis gas compressor is characterized by mainly comprising the following steps:
s1 preparation of raw material gas
The synthesis gas comes from the boundary region, and is introduced into the separation tank of the synthesis gas compressor through a stop valve, and the pressure value of the outlet of the separation tank of the synthesis gas compressor is controlled as follows: 2500-3000kPa, after the raw material gas passes through a separation tank of a synthesis gas compressor, the components are controlled in the following range according to the volume fraction ratio: h2：70-75％，N2: 20-25%, while: CO + CO2+O2≤1ppmv，Ar+CH4≤2ppmv；
S2, compressing synthetic gas
Introducing the raw material gas in the S1 into a synthesis gas centrifugal compressor, wherein the centrifugal compressor is divided into three sections, the centrifugal compressor is powered by a steam turbine, the steam turbine is connected with two surface coolers for different workload treatments in parallel, and the ratio of the charging amount of nitrogen to the charging amount of hydrogen through a bypass is as follows: 3-3.5:1, introducing synthesis gas into a centrifugal compressor, mixing a plurality of strands of gas in the centrifugal compressor, compressing the mixed gas to 14820-, the synthesis gas passing through the second-stage inlet flows to a circulating gas part of the centrifugal compressor from an inner outlet, and the circulating gas of the centrifugal compressor is cooled to 38 ℃ in two synthesis tower outlet water coolers connected in parallel at the synthesis tower outlet;
two synthesis tower outlet water coolers are connected in parallel at the outlet of the synthesis tower for the circulating gas of the synthesis gas compressor, so that a synthesis gas pipeline is led out from a main pipe of the synthesis tower outlet water cooler to be connected with the newly-added synthesis tower outlet water cooler, the synthesis gas is led away from a pipeline, the synthesis gas coming out of the synthesis tower outlet water cooler A is converged to a main pipe of the synthesis tower outlet water cooler, the circulating water pipeline of the synthesis tower outlet water cooler is connected with the circulating water pipeline of the synthesis tower outlet water cooler, and the temperature of the synthesis gas is further cooled;
s3 conversion of syngas to ammonia
Introducing the synthesis gas leaving the synthesis gas synthesis tower into an ammonia synthesis tower, wherein the space velocity of the ammonia synthesis tower is set to 8500h-1Controlling the temperature of the synthesis gas of a heat exchanger tube pass at an inlet of an ammonia synthesis tower to be between 185 and 200 ℃, then introducing the synthesis gas into a first layer bed through a plurality of lines, communicating a tube pass outlet of a heat exchanger at an outlet of the synthesis tower with a gas start-up heating furnace for raising the temperature of a catalyst bed to the reaction temperature after parking, introducing the synthesis gas into the heat exchanger tube pass of the first catalyst layer bed, carrying out heat exchange on the synthesis gas flowing to the outlet gas of the first layer bed at the moment, flowing to the top of the first layer bed and radially passing through the bed, flowing out at the bottom of the bed and directly passing through a channel to the shell pass of the heat exchanger of the first catalyst layer bed, and carrying out cold excitationThe line cold gas is not passed through the annular gap, but directly injected and mixed with the synthetic gas before the synthetic gas flows out of the first layer bed and enters the shell pass of the first catalyst layer bed heat exchanger, the ammonia gas at the outlet of the ammonia synthesis tower is further cooled to 76 ℃ at the shell pass of the first catalyst layer bed heat exchanger, the synthetic gas leaving the shell pass of the first catalyst layer bed heat exchanger flows out from the outlet of the water cooler at the outlet of the synthesis tower through the isolating valve of the circulation loop, the temperature of the synthetic gas is further reduced to 35 ℃, the cooled synthetic gas enters two small NH devices connected in parallel3Further cooling and condensing in a condenser, NH3The condenser is externally connected with an NH3Separator, tower gas and from NH3The synthesis gas returned by the separator undergoes internal heat exchange and is cooled by the cold ammonia outside the tubes, causing liquid NH to form3Boiling at two different temperatures of 14.7 ℃ and-3.2 ℃ to form NH3A rubber ball cleaning device (1) is arranged on the condenser, and prepared NH is3Separating the synthesis gas in an ammonia separator to obtain the prepared NH3The ammonia enters a flash evaporation tank, and the ammonia condensed by the synthesis loop is frozen and purified by a three-level ammonia freezing system;
the rubber ball cleaning device (1) comprises: the glue ball cleaning device comprises a plurality of glue balls (5), a ball feeding device (2) for cleaning the glue balls, a ball inlet pipe (3) and a ball outlet pipe (4) which are connected to the ball feeding device (2), and a circulating mechanism (6) for circularly cleaning circulating water inside the glue ball cleaning device (1);
the ball delivery device (2) comprises: spherical net (21), the setting of sending is in send inside ball runner (22), the setting of sending of net (21) to be in send a plurality of deflectors (23) on ball runner (22), inlet tube (3) comprises multisection spiral pipe (31), and the diameter of every section spiral pipe (31) to the direction of sending net (21) descends layer upon layer, circulation mechanism (6) include: the cleaning device comprises a circulation chamber (61), a circulation roller (62) arranged in the circulation chamber (61), a circulation liquid inlet pipe (63) arranged on the circulation chamber (61) and used for communicating with a rubber ball cleaning device (1), and a circulation liquid outlet pipe (64) arranged on the circulation chamber (61) and used for communicating with a ball conveying net (21), wherein the circulation chamber (61) pumps circulation water through a circulation pump (7), and cleaning grains (311) are engraved on each section of spiral pipe (31);
in S3, the lines for the syngas to enter the first bed are: the first one is: the synthesis gas flows from the annular space of the ammonia synthesis tower to the tube pass of the first catalyst bed heat exchanger and then flows to the first bed layer; a second bar: the synthesis gas flows into the first bed through a plurality of quenching lines; and a third: the synthesis gas flows to the first layer bed through the second catalyst layer bed heat exchanger; fourth, the method comprises the following steps: the synthesis gas passes through the coils of the start-up heater to the first bed.
2. The process of claim 1, wherein the flow rate of the synthesis gas in the second catalyst bed heat exchanger is controlled to be less than 70000kg/h, and the pressure is controlled to be: 8-15 MPa.
3. The process of claim 1, wherein the centrifugal compressor comprises a fresh gas compression section and an isolated recycle gas compression impeller, and the feed gases are mixed within the compressor.
4. The process of claim 1, wherein the second stage inlet is provided with a filter to remove impurities.
5. An apparatus for use in the process of any one of claims 1 to 4, comprising: a syngas compressor separator tank for preparing a feed gas, a syngas synthesis column for syngas compression, an ammonia synthesis column for converting syngas to ammonia, the syngas synthesis column comprising within: the synthesis gas synthesis system comprises a centrifugal compressor for mixing synthesis gas, a heat exchanger arranged at the inlet of a synthesis gas synthesis tower, a cold air bypass communicated with the heat exchanger and used for controlling the inlet temperature of the heat exchanger, a DCS control valve used for controlling the bypass, two same intermittent coolers communicated with the centrifugal compressor and arranged in parallel, and two synthesis tower outlet water coolers arranged at the outlet of the synthesis tower and arranged in parallel, wherein the inlet of the ammonia synthesis tower is also provided with the heat exchanger, and the inside of the ammonia synthesis tower comprises: NH (NH)3A condenser connected to the NH3A rubber ball cleaning device (1) on the condenser, which is externally connected with the NH3NH on condenser3A separator.
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Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1050929A (en) * | 1989-10-12 | 1991-04-24 | 湘潭大学 | Stopped pipe type fluidizing cleans and strengthening and heat transferring device |
| CN101624355A (en) * | 2009-08-10 | 2010-01-13 | 四川金圣赛瑞化工有限责任公司 | Medium-pressure recovery process of low steam/carbon ratio-three-section adsorption-evaporative ammonia-cooling carbamide production |
| WO2011026263A1 (en) * | 2009-09-01 | 2011-03-10 | Ni Yonggang | Front end seal head pipe box for water-cooling machine set shell-and-tube condenser with rubber ball on-line cleaning function |
| CN202482077U (en) * | 2012-03-16 | 2012-10-10 | 内蒙古鄂尔多斯联合化工有限公司 | Equipment capable of switching pre-tower ammonia separation system and post-tower ammonia separation system |
| CN103471453A (en) * | 2013-09-15 | 2013-12-25 | 黑龙江宏宇电站设备有限公司 | Automatic cleaning device and cleaning method for power plant condenser rubber balls |
| CN110546365A (en) * | 2017-04-06 | 2019-12-06 | 通用全球采购有限责任公司 | Method and system for a multi-stage exhaust gas cooler |
| CN210715017U (en) * | 2019-09-18 | 2020-06-09 | 江苏德翔化工机械有限公司 | Compressor knockout drum that separation effect is good |
| CN211234104U (en) * | 2019-11-07 | 2020-08-11 | 杭州绿能环保发电有限公司 | Condenser cleaning device |
-
2020
- 2020-12-21 CN CN202011518872.9A patent/CN112499583B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1050929A (en) * | 1989-10-12 | 1991-04-24 | 湘潭大学 | Stopped pipe type fluidizing cleans and strengthening and heat transferring device |
| CN101624355A (en) * | 2009-08-10 | 2010-01-13 | 四川金圣赛瑞化工有限责任公司 | Medium-pressure recovery process of low steam/carbon ratio-three-section adsorption-evaporative ammonia-cooling carbamide production |
| WO2011026263A1 (en) * | 2009-09-01 | 2011-03-10 | Ni Yonggang | Front end seal head pipe box for water-cooling machine set shell-and-tube condenser with rubber ball on-line cleaning function |
| CN202482077U (en) * | 2012-03-16 | 2012-10-10 | 内蒙古鄂尔多斯联合化工有限公司 | Equipment capable of switching pre-tower ammonia separation system and post-tower ammonia separation system |
| CN103471453A (en) * | 2013-09-15 | 2013-12-25 | 黑龙江宏宇电站设备有限公司 | Automatic cleaning device and cleaning method for power plant condenser rubber balls |
| CN110546365A (en) * | 2017-04-06 | 2019-12-06 | 通用全球采购有限责任公司 | Method and system for a multi-stage exhaust gas cooler |
| CN210715017U (en) * | 2019-09-18 | 2020-06-09 | 江苏德翔化工机械有限公司 | Compressor knockout drum that separation effect is good |
| CN211234104U (en) * | 2019-11-07 | 2020-08-11 | 杭州绿能环保发电有限公司 | Condenser cleaning device |
Non-Patent Citations (1)
| Title |
|---|
| 新型氨合成工艺技术的特点及比较;张占一;《化肥设计》;20111225;第48-52页 * |
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