CN213433047U - Single-tower open type steam stripping device for acid water conversion treatment - Google Patents
Single-tower open type steam stripping device for acid water conversion treatment Download PDFInfo
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- CN213433047U CN213433047U CN202021781938.9U CN202021781938U CN213433047U CN 213433047 U CN213433047 U CN 213433047U CN 202021781938 U CN202021781938 U CN 202021781938U CN 213433047 U CN213433047 U CN 213433047U
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Abstract
The utility model relates to a technical field of coal chemical industry transform workshop section, concretely relates to steam stripping device is opened to single tower that transform acidic water was handled. Comprises a stripping tower, a tower top condenser, a separator and a tower kettle heat exchanger; the top outlet of the stripping tower is communicated with the inlet of the pipe layer of the condenser at the top of the tower through a pipeline, and the outlet of the pipe layer of the condenser at the top of the tower is communicated with the inlet of the middle upper part of the separator through a pipeline; the shell inlet of the tower top condenser is communicated with a conversion condensate inlet, the shell outlet of the tower top condenser is communicated with the shell inlet of the tower kettle heat exchanger through a pipeline, and the shell outlet of the tower kettle heat exchanger is communicated with the top inlet of the stripping tower through a pipeline; the bottom outlet of the stripping tower is communicated with the inlet of the pipe layer of the heat exchanger at the bottom of the tower kettle through a pipeline. The utility model discloses a device has saved tower cauldron heat exchanger or top of the tower heat exchanger and need be with letting in the circulating water, directly adopts the transform condensate that needs the strip to cool off top of the tower vapour and gas and tower cauldron purification condensate as the cold source, has reached maximize energy utilization's effect, has improved the energy utilization of device.
Description
Technical Field
The utility model relates to a technical field of coal chemical industry transform workshop section, concretely relates to open steam stripping device of single tower who transforms sour water treatment.
Background
Condensate produced in the coal chemical conversion section contains a large amount of NH3、H2S、CO2And the impurities are directly discharged to pollute the underground water and the surrounding air. And the impurities are high, so that the sewage cannot be directly treated by a sewage treatment device. Generally, the NH in the gas is pretreated by a stripping device3、H2S、CO2And the impurities are stripped and separated out, so that the aim of purifying and recycling the condensate is fulfilled. Stripped NH-containing3、H2S、CO2And the tail gas with impurities is sent to a downstream device for further treatment. The steam stripping process is divided into two types according to whether the condensate is sent to the sewage treatment after the steam containing the impurities is cooled. One is that the steam condensate is sent to the sewage treatment, which is called as open-type steam stripping process, and the other is that the steam condensate is directly returned to the steam stripping tower for repeated steam stripping, which is called as closed-type steam stripping process.
In the existing single-tower steam stripping device, as shown in fig. 2, the conversion condensate is heated by the steam at the top of the tower only through the heat exchanger at the top of the tower, or heated by the liquid at the bottom of the tower through the heat exchanger at the bottom of the tower, and the purification condensate at the bottom of the tower or the gas at the top of the tower needs additional cooling media such as circulating water or desalted water to be cooled, so that the energy is not recycled, and the energy consumption is high.
SUMMERY OF THE UTILITY MODEL
Weak point to prior art exists, the utility model provides a single-tower open steam stripping device who changes sour water treatment uses feeding low temperature condensate as the cold source, and furthest's utilization is stripped the waste heat in gas and the tower cauldron condensate in back, solves the extravagant problem of steam stripping technology energy utilization, reaches the purpose that the energy high efficiency was utilized.
The specific technical scheme is as follows:
a single-tower open type stripping device for conversion acid water treatment comprises a stripping tower 1, a tower top condenser 2, a separator 3 and a tower kettle heat exchanger 4;
the top outlet of the stripping tower 1 is communicated with the inlet of the pipe layer of the overhead condenser 2 through a pipeline, the outlet of the pipe layer of the overhead condenser 2 is communicated with the inlet of the middle upper part of the separator 3 through a pipeline, the bottom outlet of the separator 3 is communicated with a downstream sewage treatment device, and the top outlet of the separator 3 is communicated with a downstream acid gas treatment device;
the shell inlet of the tower top condenser 2 is communicated with a conversion condensate inlet, the shell outlet of the tower top condenser 2 is communicated with the shell inlet of the tower kettle heat exchanger 4 through a pipeline, and the shell outlet of the tower kettle heat exchanger 4 is communicated with the top inlet of the stripping tower 1 through a pipeline;
the outlet at the bottom of the stripping tower 1 is communicated with the inlet of the layer 4 of the tower kettle heat exchanger through a pipeline, and the outlet of the layer 4 of the tower kettle heat exchanger is communicated with a downstream processing device.
Further, the design temperature of the overhead condenser 2 is 180 ℃ and the design pressure is 1.0 MPaG; the design temperature of the column bottom heat exchanger 4 is 180 ℃, and the design pressure is 1.0 MPaG.
Further, the design temperature of the separator 3 is 130 ℃, the design pressure is 0.6 MPaG, and the top of the separator 3 is provided with a wire mesh.
The utility model has the advantages of as follows:
the single-tower open type stripping device of the utility model omits the step that the heat exchanger at the tower bottom or the heat exchanger at the tower top needs to be cooled by circulating water, namely, the circulating water is not consumed; the conversion condensate needing steam stripping is directly used as a cold source to cool the steam stripping gas at the top of the tower and the purification condensate at the bottom of the tower, so that the effect of maximizing energy utilization is achieved, the energy utilization rate of the device is improved, the energy consumption of the device is reduced, and the operating cost of the device is saved. By taking 40000 kg/h of condensate of the treatment process, the temperature of 40 ℃ and the pressure of 0.5 MPaG as examples, compared with the traditional device, the device of the utility model can reduce 3500 kg/h of consumed steam and 63.8 t/h of consumed circulating water; simultaneously the utility model discloses an open stripping apparatus of single tower has saved the configuration of pipe fittings such as valves on external circulating water pipeline and the pipeline owing to adopt transform condensate self as the cold source, has saved the device pipeline investment.
Drawings
Fig. 1 is a schematic structural view of a single-tower open stripping device of the present invention.
FIG. 2 is a schematic diagram of a single column open stripping apparatus of the prior art.
Wherein: a stripping tower 1, a tower top condenser 2, a separator 3 and a tower bottom heat exchanger 4.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the detailed description and specific examples, while indicating the invention, are intended for purposes of illustration only and are not intended to limit the scope of the invention.
Examples
A single-tower open type stripping device for conversion acid water treatment comprises a stripping tower 1, a tower top condenser 2, a separator 3 and a tower kettle heat exchanger 4;
the top outlet of the stripping tower 1 is communicated with the inlet of the pipe layer of the overhead condenser 2 through a pipeline, the outlet of the pipe layer of the overhead condenser 2 is communicated with the inlet of the middle upper part of the separator 3 through a pipeline, the bottom outlet of the separator 3 is communicated with a downstream sewage treatment device, and the top outlet of the separator 3 is communicated with a downstream acid gas treatment device;
the shell inlet of the tower top condenser 2 is communicated with a conversion condensate inlet, the shell outlet of the tower top condenser 2 is communicated with the shell inlet of the tower kettle heat exchanger 4 through a pipeline, and the shell outlet of the tower kettle heat exchanger 4 is communicated with the top inlet of the stripping tower 1 through a pipeline;
the outlet at the bottom of the stripping tower 1 is communicated with the inlet of the layer 4 of the tower kettle heat exchanger through a pipeline, and the outlet of the layer 4 of the tower kettle heat exchanger is communicated with a downstream processing device.
The design temperature of the overhead condenser 2 is 180 ℃, and the design pressure is 1.0 MPaG; the design temperature of the column bottom heat exchanger 4 is 180 ℃, and the design pressure is 1.0 MPaG.
The design temperature of the separator 3 is 130 ℃, the design pressure is 0.6 MPaG, and the top of the separator 3 is provided with a wire mesh.
The process method for converting the stripping energy of the acid water based on the device comprises the following procedures:
step (1), a primary heat exchange process:
introducing condensate into the overhead condenser (2), and exchanging heat between the condensate and the stripping gas discharged from the top outlet of the stripping tower (1) in the overhead condenser (2) to obtain primary heat exchange condensate and stripping condensate, wherein the condensate has the temperature of 40 ℃ and the pressure of 0.6 MPaG, and the main components are as follows: h2O 99.88%，CO2 0.11%，H2S 65 ppm，NH3 0.013%， H2 5.6 ppm，CO 9.3 ppm，COS 5.6 ppm，N22.9 ppm (mass fraction, composition will vary depending on coal quality, but not order of magnitude). The design temperature of the overhead condenser (2) was 180 ℃ and the design pressure was 1.0 MPaG. The temperature of the primary heat exchange condensate is about 70 ℃, the pressure is 0.55 MPaG, and the main components are unchanged; the temperature of the stripping condensate is 110 ℃, and the pressure is 0.3 MPaG, and the stripping condensate mainly comprises the following components: h2O 97.88%，CO2 1.8%，H2S 0.11%，NH3 0.11%， H2 9.5 ppm，CO 15.8 ppm，COS 9.4 ppm，N24.9 ppm (mass fraction, composition will vary depending on coal quality, but not order of magnitude).
Step (2) secondary heat exchange process:
the method comprises the following steps that a primary heat exchange condensate enters a tower kettle heat exchanger (4), the primary heat exchange condensate and a purification condensate discharged from the bottom of a stripping tower (1) exchange heat in the tower kettle heat exchanger (4) to obtain a secondary heat exchange condensate and a purification condensate, wherein the design temperature of the tower kettle heat exchanger (4) is 180 ℃, the design pressure is 1.0 MPaG, the temperature of the secondary heat exchange condensate is 100 ℃, the pressure is 0.5 MPaG, and the primary heat exchange condensate is the same: h2O 99.88%，CO2 0.11%，H2S 65 ppm，NH3 0.013%， H2 5.6 ppm，CO 9.3 ppm，COS 5.6 ppm，N22.9 ppm (mass fraction); the temperature of the purification condensate is 120 ℃, and the pressure is 0.3 MPaG, and the main components are as follows: h2O 99.99%， NH3<50 ppm (mass fraction); purifying gelThe liquid is discharged from the tower kettle heat exchanger (4) and then is sent out of a stripping device for reuse through pressurization by a pump.
And (3) a separation process:
the stripping condensate enters a separator (3) and is separated to obtain acid gas and stripping sewage, and the acid gas comprises the following main components: h2O 33.81%，CO2 61.87%，H2S 3.01%，NH3 0.22%， H2 0.97%，CO 972 ppm，COS 22 ppm，N20.03% (volume fraction); the stripping sewage comprises the following components: h2O 99.25%，CO2 0.47%，H2S 61.80 ppm，NH3 0.21%，CO 2.56 ppm，COS 8.96 ppm，N20.75 ppm (mass fraction); the acid gas passes through a desulfurizing and recycling device at the top of the separator (3), and the stripped sewage at the bottom of the separator (3) is sent to a sewage treatment station for treatment; the design temperature of the separator (3) is 130 ℃, the design pressure is 0.6 MPaG, and the top of the separator (3) is provided with a wire mesh for separating liquid drops in the stripping gas.
Step (4) stripping:
introducing low-pressure steam into the lower part of the stripping tower (1), contacting the secondary heat exchange condensate introduced into the top of the stripping tower (1) by the low-pressure steam, stripping to obtain purified condensate and stripping gas, introducing the purified condensate into a tube layer inlet of the tower kettle heat exchanger (4) through a pipeline, and introducing the stripping gas into a tube layer inlet of the tower top heat exchanger from the top of the stripping tower (1);
wherein the temperature of the purification condensate is 145 ℃, the pressure is 0.35 MPaG, and the main components are as follows: h2O 99.99%， NH3<50 ppm (mass fraction), temperature of stripping gas 145 deg.C, pressure 0.33 MPaG, main component H2O 98.96%，CO2 0.74%，H2S 0.059%，NH3 0.23%， H2 86 ppm，CO 10 ppm，COS 2.86 ppm，N23.16 ppm (volume fraction).
Taking a coal-to-methanol project of 60 ten thousand tons/year as an example, the annual operating time is 8000 hours.
40000 kg/h of condensate in the treatment process of the project, the temperature is 40 ℃, the pressure is 0.5 MPaG, and according to the conventional single-tower open type steam stripping process, 8000 kg/h of saturated steam of 0.5 MPaG is consumed for treating the condensate: circulating water at 30 ℃ is 63.8 t/h; by adopting the device and the process method of the utility model, only 4500 kg/h of 0.5 MPaG saturated steam is needed to be consumed, and circulating water is not consumed. Namely, compared with the traditional process, the utility model can reduce the consumption of steam by 3500 kg/h and the consumption of circulating water by 63.8 t/h.
According to the petrochemical engineering design energy consumption calculation standard (GB/T50441-2016), the energy consumption reduction is equivalent to 234.8 kg of standard oil/h, and the energy consumption saving per year is equivalent to 1878.4 tons of standard oil; according to the general rule of comprehensive energy consumption calculation (GB/T2589-2008), the energy consumption reduction is equivalent to 335.4 kg of standard coal per hour, and the energy consumption saving per year is equivalent to 2683.2 tons of standard coal. According to steam 100 yuan/ton, circulating water 0.6 yuan/ton calculates, uses the utility model discloses a technology can save the working costs 310.62 ten thousand yuan each year.
Claims (3)
1. The utility model provides a single tower open stripping device of transform acid water treatment which characterized in that: the single-tower open type stripping device comprises a stripping tower (1), a tower top condenser (2), a separator (3) and a tower kettle heat exchanger (4);
the top outlet of the stripping tower (1) is communicated with the pipe layer inlet of the overhead condenser (2) through a pipeline, the pipe layer outlet of the overhead condenser (2) is communicated with the middle upper inlet of the separator (3) through a pipeline, the bottom outlet of the separator (3) is communicated with a downstream sewage treatment device, and the top outlet of the separator (3) is communicated with a downstream acid gas treatment device;
a shell layer inlet of the tower top condenser (2) is communicated with a conversion condensate inlet, a shell layer outlet of the tower top condenser (2) is communicated with a shell layer inlet of the tower kettle heat exchanger (4) through a pipeline, and a shell layer outlet of the tower kettle heat exchanger (4) is communicated with a top inlet of the stripping tower (1) through a pipeline;
the bottom outlet of the stripping tower (1) is communicated with the pipe layer inlet of the tower kettle heat exchanger (4) through a pipeline, and the pipe layer outlet of the tower kettle heat exchanger (4) is communicated with a downstream processing device.
2. The single-column open stripping apparatus for sour water shift treatment according to claim 1, characterized in that: the design temperature of the overhead condenser (2) is 180 ℃, and the design pressure is 1.0 MPaG; the design temperature of the tower kettle heat exchanger (4) is 180 ℃, and the design pressure is 1.0 MPaG.
3. The single-column open stripping apparatus for sour water shift treatment according to claim 1, characterized in that: the design temperature of the separator (3) is 130 ℃, the design pressure is 0.6 MPaG, and the top of the separator (3) is provided with a wire mesh.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113952752A (en) * | 2021-10-28 | 2022-01-21 | 镇海石化工程股份有限公司 | Anti-corrosion condensation method for tower top of acidic water stripping device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113952752A (en) * | 2021-10-28 | 2022-01-21 | 镇海石化工程股份有限公司 | Anti-corrosion condensation method for tower top of acidic water stripping device |
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