CN111040815B - Desalting and corrosion preventing system of depentanizer - Google Patents
Desalting and corrosion preventing system of depentanizer Download PDFInfo
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- CN111040815B CN111040815B CN201911311892.6A CN201911311892A CN111040815B CN 111040815 B CN111040815 B CN 111040815B CN 201911311892 A CN201911311892 A CN 201911311892A CN 111040815 B CN111040815 B CN 111040815B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G75/00—Inhibiting corrosion or fouling in apparatus for treatment or conversion of hydrocarbon oils, in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/10—Inhibiting corrosion during distillation
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Abstract
The invention relates to a desalting and corrosion preventing system of a depentanizer, which is used for removing ammonium salt crystals in the depentanizer. The device comprises a depentanizer, wherein a feeding line is connected to the side wall of one side of the depentanizer, one end of the feeding line is connected with the depentanizer, the other end of the feeding line is connected with the bottom end of a dechlorination tank, a heat exchanger is arranged on the feeding line between the dechlorination tank and the depentanizer, the bottom of the depentanizer is connected into the heat exchanger through a pipeline, a water outlet pipe of the heat exchanger is provided with branches, one branch pipeline is connected to a liquefied gas absorption tank, and the other branch pipeline is connected to an unqualified storage tank; and the heat exchanger is provided with a guide shower valve group through a pipeline, and a connecting port of the guide shower valve group is connected with a metering pump through a pipeline. The key point of the invention is that the ammonium chloride crystal is removed by on-line small-flow water injection; thereby recovering the separation precision problem of C201 and ensuring that the sample without fluctuation of the tower is qualified. Reducing the formation of ammonium chloride; the advantages are that the water is injected on line without shutdown treatment, and the water can be injected at any time to remove the crystal. Is beneficial to the long, stable and excellent operation of the device.
Description
Technical Field
The invention relates to a desalting and corrosion preventing system of a reforming dechlorination tank, in particular to a desalting and corrosion preventing system of a depentanizer, which is used for removing ammonium salt crystals in the depentanizer.
Background
The separation precision is reduced due to salt deposition of the depentanizer, so that light components (C5-) at the tower bottom are increased, benzene (B) is carried in the tower top, a sample at the tower top and the tower bottom is unqualified, the pressure drop of the tower is increased, the temperature at the tower top is unstable, and the liquid level fluctuation of a reflux tank is large when the temperature is serious.
The existing method for removing ammonium salt crystals in a depentanizer is that a metering pump and a water tank are added at the feeding position of the depentanizer, ammonium salt crystals on trays and pipe walls are removed from the top of a C-201 depentanizer, materials entering the depentanizer descend layer by layer along with tower plates in the depentanizer, energy exchange is carried out between the materials and light components from the bottom of the tower, partial materials or dissolved trace oxygen is vaporized, the materials enter an air cooler A-206 through the top of the tower and are cooled to about 45 ℃, partial light components are changed into liquid again and enter a reflux tank D-206, non-condensable gas is sent to a fuel gas system in front of a heating furnace through a PIC2067A/B control valve, and the materials in the reflux tank are sent to the C-201 depentanizer again through a reflux pump. Light hydrocarbon at the top of the depentanizer C-201 is mixed with the overhead oil of the prehydrogenation naphtha separating tower C-102, and enters a C4/C5 separating tower after heat exchange between E-211A/B and the bottom material of the C4/C5 separating tower. The tower top material is condensed and cooled by an air cooler A-206 and a water cooler E-209A/B and then enters a tower top reflux tank D-207, the gas at the top of the tank is discharged into a fuel gas pipe network of the device, the liquid at the bottom of the reflux tank is boosted by a pump P-205, one part of the liquid is used as reflux to flow to the top of the tower, and the other part of the liquid is used as a liquefied gas product to be sent out of the device. The bottom oil of the C4/C5 separation tower, namely pentane oil, is subjected to heat exchange with the feed through E-211A/B and is cooled through a water cooler E-212A/B, and then the pentane oil is taken as a product and sent out of the device.
The method has long process, needs shutdown treatment and cannot realize long-time stable operation; in the prior art, the chlorine content of the catalyst of the reforming device is controlled to be 1.1 percent, and the chlorine content in the gas is 4-6ppm and is higher, which is probably an important reason for salt deposition; the corrosion mechanism is as follows:
NH4CL+H2O NH3+HCL
H2O+ HCL H+CL
Fe+CL FeCL2。
in the prior art, the depentanizer is cut off or the reforming unit is shut down, and then the depentanizer is washed by a large amount of water for 1 to 2 days, and then the chlorine content of the water bag of the reflux tank is qualified after sampling analysis, wherein the chlorine content of the water bag is less than 100 PPM. High cost and easy environmental pollution.
The existing resources which utilize the ammonium salt removal crystallization mode are not developed for redistribution and reconstruction.
Disclosure of Invention
In view of the technical defects, the invention aims to provide a desalination and corrosion prevention system of a depentanizer, which is used for removing ammonium chloride crystals in the depentanizer by injecting water on line, recovering the separation precision of a C201 tower and ensuring that a sample at the bottom and the top of the tower is qualified.
In order to achieve the purpose, the invention adopts the technical scheme that: the desalting and corrosion preventing system of the depentanizer comprises the depentanizer, wherein a feeding line is connected to the side wall of one side of the depentanizer, one end of the feeding line is connected with the depentanizer, the other end of the feeding line is connected with the bottom end of a dechlorination tank, a heat exchanger is arranged on the feeding line between the dechlorination tank and the depentanizer, the bottom of the depentanizer is connected into the heat exchanger through a pipeline, a water outlet pipe of the heat exchanger is provided with branches, one branch pipeline is connected to a liquefied gas absorption tank, and the other branch pipeline is connected to an unqualified storage tank; a guide shower valve group is arranged on the heat exchanger through a pipeline, and a connecting port of the guide shower valve group is connected with a metering pump through a pipeline;
the guide shower valve groups are in parallel connection, the number of the guide shower valve groups is 2, and the guide shower valve groups are respectively arranged in a clear row and a close row; 2 water injection lines are arranged to meet design requirements
The guide shower valves arranged in the open row and the guide shower valves arranged in the close row are respectively connected with the metering pump through pipelines;
the number of the metering pumps is 2, water is injected through the metering pumps, reaches the heat exchanger through the pilot valve, and enters the depentanizer through a feed line connected with the heat exchanger after heat exchange of the heat exchanger;
furthermore, the heat exchanger is used for primary heat exchange, and in order to achieve a better heat exchange effect, a secondary heat exchanger and a tertiary heat exchanger are connected in series at the rear end of the primary heat exchanger; a feeding pipeline from the bottom of the dechlorination tank to a feeding port of the depentanizer is connected to the primary heat exchanger; the bottom pipeline of the depentanizer is sequentially connected with a hot water pipe of a first-stage heat exchanger, the water outlet end of the hot water pipe is connected into a cold water pipe of a second-stage heat exchanger, after heat exchange is carried out through the hot water pipe in the second-stage heat exchanger, the water outlet end of the hot water pipe is connected into a hot water pipe of a third-stage heat exchanger, after heat exchange is carried out in the third-stage heat exchanger, the water outlet end of the hot water end of the heat exchanger is sequentially connected with a control valve group and a reflux pump, and is connected into a liquefied gas absorption tank through the reflux pump, so that three-stage heat exchange is completed, and a required heat exchange effect is achieved;
the water outlet end of the cold water pipe of the secondary heat exchanger is connected to the water inlet end of the cold water pipe of the tertiary heat exchanger, and the water outlet end of the cold water pipe of the tertiary heat exchanger is connected to an unqualified storage tank and a subsequent tower;
the desalting process of the depentanizer comprises the following steps:
opening a valve FV-2058, the material reacted in the dechlorination tank R206 reaches a first-level heat exchanger through a feed line for heat exchange, the material after heat exchange enters a depentanizer, the material entering the tower descends layer by layer along with a tower plate in the tower, exchanges energy with light components from the bottom of the tower, part of the material or dissolved trace oxygen is vaporized, the material enters an air cooler A-203 through the top of the tower for cooling and after heat exchange, part of the light components are changed into liquid again and enter a reflux tank D206, non-condensable gas is respectively sent to a fuel gas system in front of a heating furnace through a PV2067A/B control valve, and the material in the reflux tank D206 is sent to the C-201 tower again through a reflux pump P-203A/B;
materials in the C-201 tower enter the tower again after heat exchange through heat exchangers E-208A/B arranged at two sides of the tower, enter a first-stage heat exchanger, a second-stage heat exchanger and a third-stage heat exchanger from a tower bottom pipeline for heat exchange, and are sent into a liquefied gas absorption tank D205 through a reflux pump P-202A/B after heat exchange; part of the liquefied gas reaches a liquefied gas absorption tank D205 and flows back to the depentanizer for circulation under the action of a reflux pump P-203A/B through a pipeline;
when the ammonium salt crystallization needs to be removed, a pilot valve and a metering pump at the position of a first-stage heat exchanger are opened, water is injected into the metering pump, and the water passes through a cold water pipeline of the first-stage heat exchanger and reaches a depentanizer through a feed line, so that the inside of the depentanizer is cleaned, and the ammonium chloride is removed.
The flow rate of the on-line water injection is less than 1 t/h;
the key point of the invention is that the ammonium chloride crystal is removed by on-line small-flow water injection; thereby recovering the separation precision problem of C201 and ensuring that the sample without fluctuation of the tower is qualified. Reducing the formation of ammonium chloride; the advantages are that the water is injected on line without shutdown treatment, and the water can be injected at any time to remove the crystal. Is beneficial to the long, stable and excellent operation of the device.
Drawings
FIG. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a partial detailed view of fig. 1.
In the figure, 1, a depentanizer, 2, a feed line, 3, a dechlorination tank, 4, a primary heat exchanger, 5, a liquefied gas absorption tank, 6, a unqualified storage tank, 7, a bright row guide shower valve, 8, a close row guide shower valve, 9, a metering pump, 10, a secondary heat exchanger, 11, a tertiary heat exchanger, 12, control valve groups FV-2017, 13, reflux pumps P-202A/B, 14, air coolers A-203, 15, reflux tanks D206, 16, control valves PV2067A/B, 17, a fuel gas system before a heating furnace, 18, reflux pumps P-203A/B, 19 and a heat exchanger E-208A/B.
Detailed Description
The present invention will be described in detail with reference to the accompanying drawings.
As shown in fig. 1-2, the desalination and corrosion prevention system of the depentanizer comprises a depentanizer 1, wherein a feeding line 2 is connected to the side wall of one side of the depentanizer 1, one end of the feeding line 2 is connected with the depentanizer 1, the other end of the feeding line is connected with the bottom end of a dechlorination tank 3, a heat exchanger is arranged on the feeding line 2 between the dechlorination tank 3 and the depentanizer 1, the bottom of the depentanizer 1 is connected into the heat exchanger through a pipeline, a water outlet pipe of the heat exchanger is provided with branches, one branch pipeline is connected to a liquefied gas absorption tank 5, and the other branch pipeline is connected to an unqualified storage tank 6; a guide shower valve group is arranged on the heat exchanger through a pipeline, and a connecting port of the guide shower valve group is connected with a metering pump 9 through a pipeline;
the guide shower valve groups are in parallel connection, the number of the guide shower valve groups is 2, and the guide shower valve groups are respectively arranged in a clear row and a close row;
the guide shower valves 7 arranged in the open row and the guide shower valves 8 arranged in the close row are respectively connected with metering pumps 9 through pipelines, the number of the metering pumps 9 is 2, water is injected through the metering pumps 9, the water reaches a heat exchanger through the guide shower valves, and after heat exchange of the heat exchanger, the water enters the depentanizer 1 through a feeding line 2 connected with the heat exchanger;
further, the heat exchanger is a primary heat exchange heat exchanger 4, and in order to achieve a better heat exchange effect, a secondary heat exchanger 10 and a tertiary heat exchanger 11 are connected in series at the rear end of the primary heat exchanger 4; a feeding pipeline from the bottom of the dechlorination tank 3 to a feeding port of the depentanizer 1 is connected to the primary heat exchanger 4; the bottom pipeline of the depentanizer 1 is sequentially connected with a hot water pipe of a first-stage heat exchanger 4, the water outlet end of the hot water pipe is connected with a cold water pipe of a second-stage heat exchanger 10, after heat exchange is carried out through a hot water pipe inside the second-stage heat exchanger 10, the water outlet end of the hot water pipe is connected with a hot water pipe of a third-stage heat exchanger 11, after heat exchange is carried out inside the third-stage heat exchanger 11, the water outlet end of the hot water end of the heat exchanger is sequentially connected with a control valve group 12 and a reflux pump 13 and is connected into the liquefied gas absorption tank 5 through the reflux pump 13, so that three-stage heat exchange is completed, and a required heat exchange effect is achieved; the water outlet end of the cold water pipe of the secondary heat exchanger 10 is connected with the water inlet end of the cold water pipe of the tertiary heat exchanger 11, and the water outlet end of the cold water pipe of the tertiary heat exchanger 11 is connected to the unqualified storage tank 6 and the subsequent tower;
the desalting process of the depentanizer comprises the following steps:
opening a valve FV-2058, the material reacted in the R206 dechlorination tank 3 reaches a first-stage heat exchanger 4 through a feed line 2 for heat exchange, the material after heat exchange enters a depentanizer 1, the material entering the tower descends layer by layer along with a tower plate in the tower, exchanges energy with light components from the bottom of the tower, part of the material or dissolved trace oxygen is vaporized, the material enters an A-203 air cooler 14 through the top of the tower for cooling and after heat exchange, part of the light components turns into liquid again and enters a D206 reflux tank 15, non-condensable gas is respectively sent to a fuel gas system 17 in front of a heating furnace through a PV2067A/B control valve, and the material in the reflux tank 15 is sent to the C-201 tower again through a reflux pump P-203A/B;
materials in the C-201 tower enter the tower again after heat exchange through heat exchangers E-208A/B arranged at two sides of the tower, enter a first-stage heat exchanger, a second-stage heat exchanger and a third-stage heat exchanger from a tower bottom pipeline for heat exchange, and are sent into a liquefied gas absorption tank D205 through a reflux pump P-202A/B after heat exchange; part of the liquefied gas reaches a liquefied gas absorption tank D205 and flows back to the depentanizer 1 for circulation under the action of a reflux pump P-203A/B through a pipeline;
when ammonium salt crystallization needs to be removed, a pilot valve and a metering pump 9 at the position of a primary heat exchanger 4 are opened, water is injected into the metering pump 9, the flow rate of the on-line injected water is less than 1t/h, the water passes through a cold water pipeline of the primary heat exchanger 4 and reaches the inside of a depentanizer 1 through a feed line 2, and therefore the inside of the depentanizer is cleaned, and ammonium chloride is removed.
Claims (8)
1. The desalting and corrosion preventing system of the depentanizer is characterized in that: the device comprises a depentanizer, wherein a feeding line is connected to the side wall of one side of the depentanizer, one end of the feeding line is connected with the depentanizer, the other end of the feeding line is connected with the bottom end of a dechlorination tank, a heat exchanger is arranged on the feeding line between the dechlorination tank and the depentanizer, the bottom of the depentanizer is connected into the heat exchanger through a pipeline, a water outlet pipe of the heat exchanger is provided with branches, one branch pipeline is connected to a liquefied gas absorption tank, and the other branch pipeline is connected to an unqualified storage tank; a guide shower valve group is arranged on the heat exchanger through a pipeline, and a connecting port of the guide shower valve group is connected with a metering pump through a pipeline; when ammonium salt crystallization needs to be removed, a pilot valve and a metering pump at the position of the primary heat exchanger are opened, water is injected into the metering pump, the flow rate of the on-line water injection is less than 1t/h, and the water reaches the depentanizer through a cold water pipeline of the primary heat exchanger through a feed line.
2. The depentanizer desalination corrosion protection system of claim 1, wherein: the guide shower valve group is in parallel connection, the number of the guide shower valve group is 2, and the guide shower valve group is respectively arranged in a clear row and a close row.
3. The depentanizer desalination corrosion protection system of claim 2, wherein: the guide shower valve arranged on the bright row and the guide shower valve arranged on the dark row are respectively connected with the metering pump through pipelines.
4. The depentanizer desalination corrosion protection system of claim 3, wherein: the quantity of the metering pumps is 2, water is injected through the metering pumps, reaches the heat exchanger through the pilot valve, and enters the depentanizer through a feed line connected with the heat exchanger after heat exchange of the heat exchanger.
5. The depentanizer desalination corrosion protection system of claim 1, wherein: the heat exchanger is used for primary heat exchange, and a secondary heat exchanger and a tertiary heat exchanger are connected in series at the rear end of the primary heat exchanger; a feeding pipeline from the bottom of the dechlorination tank to a feeding port of the depentanizer is connected to the primary heat exchanger; the bottom pipeline of the depentanizer is sequentially connected with a first-stage heat exchanger hot water pipe, the water outlet end of the hot water pipe is connected into a second-stage heat exchanger cold water pipe, after heat exchange is carried out through a hot water pipe in the second-stage heat exchanger, the water outlet end of the hot water pipe is connected into a third-stage heat exchanger hot water pipe, after heat exchange is carried out in the third-stage heat exchanger, the water outlet end of the heat exchanger hot water pipe is sequentially connected with a control valve group and a lifting pump, and the control valve group and the lifting pump are connected into a liquefied gas absorption tank through the lifting pump, so that third-stage heat exchange is completed.
6. The depentanizer desalination corrosion protection system of claim 5, wherein: and the water outlet end of the cold water pipe of the secondary heat exchanger is connected to the water inlet end of the cold water pipe of the tertiary heat exchanger, and the water outlet end of the cold water pipe of the tertiary heat exchanger is connected to an unqualified storage tank and a subsequent tower.
7. The depentanizer desalination and corrosion protection system according to any one of claims 1-5, characterized in that: the desalting process of the depentanizer comprises the following steps:
opening a valve FV-2058, the material reacted in the dechlorination tank R206 reaches a first-level heat exchanger through a feed line for heat exchange, the material after heat exchange enters a depentanizer, the material entering the tower descends layer by layer along with a tower plate in the tower, exchanges energy with light components from the bottom of the tower, part of the material or dissolved trace oxygen is vaporized, the material enters an air cooler A-203 through the top of the tower for cooling and after heat exchange, part of the light components are changed into liquid again and enter a reflux tank D206, non-condensable gas is respectively sent to a fuel gas system in front of a heating furnace through a PV2067A/B control valve, and the material in the reflux tank D206 is sent to the C-201 tower again through a reflux pump P-203A/B;
materials in the C-201 tower enter the tower again after heat exchange through heat exchangers E-208A/B arranged at two sides of the tower, enter a first-stage heat exchanger, a second-stage heat exchanger and a third-stage heat exchanger from a tower bottom pipeline for heat exchange, and are sent into a liquefied gas absorption tank D205 through a reflux pump P-202A/B after heat exchange; part of the liquefied gas reaches a liquefied gas absorption tank D205 and flows back to the depentanizer for circulation under the action of a reflux pump P-203A/B through a pipeline;
when the ammonium salt crystallization needs to be removed, a pilot valve and a metering pump at the position of a first-stage heat exchanger are opened, water is injected into the metering pump, and the water passes through a cold water pipeline of the first-stage heat exchanger and reaches a depentanizer through a feed line, so that the inside of the depentanizer is cleaned, and the ammonium chloride is removed.
8. The depentanizer desalination corrosion protection system of claim 7, wherein: the flow rate of the on-line water injection in the metering pump is less than 1 t/h.
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