CN112480974A - Process for removing peculiar smell of coal gasification vent gas - Google Patents

Process for removing peculiar smell of coal gasification vent gas Download PDF

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Publication number
CN112480974A
CN112480974A CN202011172404.0A CN202011172404A CN112480974A CN 112480974 A CN112480974 A CN 112480974A CN 202011172404 A CN202011172404 A CN 202011172404A CN 112480974 A CN112480974 A CN 112480974A
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alkali liquor
separation tank
vacuum pump
gas
exhaust gas
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闫晓洋
张薇
张炜
黄习兵
宋怡
严东
褚永良
潘怀民
郑鹏
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Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
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Sinopec Engineering Group Co Ltd
Sinopec Ningbo Engineering Co Ltd
Sinopec Ningbo Technology Research Institute
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/002—Removal of contaminants
    • C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
    • C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors

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  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

The invention relates to a process for removing peculiar smell of coal gasification vent gas. The alkali liquor absorption tower is arranged at the downstream of the vacuum pump separation tank and is provided with an input port for inputting the exhaust gas of the vacuum pump separation tank, an output port for outputting qualified exhaust gas is arranged at the top, and rich H is arranged at the bottom2And S is a liquid outlet for inputting alkali liquor. The invention effectively removes H in the exhaust gas of the vacuum pump by washing with alkali liquor2S, the problem of peculiar smell of the exhaust gas is eliminated, and the field operation environment is improved; the method has the advantages of simple process flow, less added equipment, lower investment and operation cost, small system pressure drop, no need of higher pressure of the exhaust gas, no need of additionally adding a control scheme, small equipment occupation area and higher flexibility.

Description

Process for removing peculiar smell of coal gasification vent gas
Technical Field
The invention relates to a process for removing peculiar smell of coal gasification vent gas.
Background
With the development of chemical technology and the adjustment of energy structure, coal resources have gradually become the main raw materials of chemical industry aiming at the resource structure of rich coal, poor oil and less gas in China. At present, most of hydrogen production, synthetic ammonia, MTO, MTP, SNG and the like adopt a high-efficiency and environment-friendly pressurized entrained flow coal gasification technology as a source. In the coal gasification process, coal water slurry gasification and pulverized coal gasification are included, and in order to treat solid-containing grey water, a multi-stage flash evaporation system is adopted to concentrate the grey water, so that the aim of solid-liquid separation is achieved through filtering equipment. In the coal gasification process, sulfide in the raw material coal is reacted to generate H2S and COS, etc. Most of H2S enters a purifying device along with the crude synthesis gas, is removed in a low-temperature methanol washing unit, and is concentrated into high-concentration H2And S, then sending the sulfur product into a sulfur recovery device. Small fraction of H produced by gasification2Chilling and washing of S in synthetic gasThe water enters a water system in the washing process and the like. In the flash evaporation system, both coal water slurry and pulverized coal gasification are provided with vacuum flash evaporators. The vacuum degree of the vacuum flash tank is realized by a vacuum pump, and gas pumped by the vacuum pump is discharged to the atmosphere after gas-liquid separation is carried out on the gas through a vacuum pump separation tank. Taking a certain item as an example, the discharge amount is about 0.05kg/h, and the discharge height is 25 m. Although the value is far lower than the GB/T14554 requirement of emission standard of malodorous pollutants (when the emission height is 25m, the emission standard value is 0.9 kg/h). But due to H2The S threshold is lower and is 15mg/m3(about 10 ppmwt). In the running process of the device, peculiar smell exists in the operation area of the tank top, and the field operation environment is seriously influenced. The vent gas has small gas quantity, low pressure and H2Low S concentration.
At present, in the entrained flow coal gasification technology commonly used in China, the discharged gas of a vacuum pump is usually subjected to direct emptying treatment, so that the problem of peculiar smell in a part of the device area to a certain degree is caused, and the field operation environment is influenced.
In order to solve the above problems, chinese patent CN 104248907B provides a sulfur-containing tail gas H2S tail gas purifying process, which mainly adopts limestone emulsion to purify CO in sulfur-containing tail gas2Removing solid particle impurities, and separating with gas-liquid separator and gas-liquid separator2S gas is purified, and the effect of purifying tail gas is achieved. However, the method has the disadvantages of long process, more equipment which needs to be added, large investment, suitability for treating tail gas with large gas amount and certain pressure, and inapplicability to the problems to be solved by the method. Patent application CN105329861A designs a process for preparing sulfuric acid by using industrial low-concentration sulfur-containing tail gas, and concretely relates to a process for preparing sulfuric acid by mixing sulfur-containing tail gas with air, then passing the mixture through an oxidation reactor (600-1200 ℃), combusting the mixture, and converting sulfur-containing components into SO2And then carrying out catalytic oxidation reaction on the SO through the catalyst layer2Oxidation to SO3Further to prepare sulfuric acid. Although this technique can achieve higher H2The S removal rate, but needs to increase a combustion reactor operated at high temperature and an expensive catalyst, and has high device investment and high energy consumption.Small amount of such gas, H, for treating the exhaust gas of a vacuum pump2The sulfur-containing tail gas with low S concentration has no adaptability, and the reaction temperature is high, so that the operation risk point of the device is increased.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method for effectively removing H in the exhaust gas of a vacuum pump by washing with alkali liquor in order to solve the current situation of the prior art2S, the peculiar smell of the discharged gas is eliminated, the site operation environment is improved, and the process is low in investment and operation cost, small in system pressure drop and high in flexibility.
The technical scheme adopted by the invention for solving the technical problems is as follows: a process for removing odor of coal gasification vent gas is characterized by comprising the following steps:
the adopted process system comprises
The vacuum flash evaporation separation tank is provided with an input port for inputting vacuum flash evaporation gas, the top of the vacuum flash evaporation separation tank is provided with an air outlet for outputting the flash evaporation gas, and the bottom of the vacuum flash evaporation separation tank is provided with a liquid outlet for discharging condensate;
the vacuum pump is arranged at the air outlet of the vacuum flash separation tank;
the vacuum pump separation tank is provided with an inlet for inputting flash steam output from the top of the vacuum flash separation tank, the top of the vacuum pump separation tank is provided with an outlet for outputting exhaust gas of the vacuum pump separation tank, and the bottom of the vacuum pump separation tank is provided with a liquid outlet for discharging condensate;
an alkali liquor absorption tower arranged at the downstream of the vacuum pump separation tank and provided with an input port for inputting the exhaust gas of the vacuum pump separation tank, an output port for outputting qualified exhaust gas at the top and a rich H supply at the bottom2A liquid outlet for inputting the S alkali liquor,
alkali liquor storage tank with supply of rich H2An inlet for inputting S alkali liquor, and an inlet at the top for inputting H2S, a discharge port which is emptied to a safe place, and the bottom of the discharge port are connected with a pipeline for alkali liquor to flow back from the upper part of the alkali liquor absorption tower, and an alkali liquor circulating pump is arranged on the pipeline;
the process method comprises
(1) According to the temperature, pressure, flow and H of the vent gas2S content, in the zone of the bonding apparatusDetermining the most suitable washing alkali liquor according to the configuration of alkali liquor used by a process device or other auxiliary facilities and the configuration of a rich liquor centralized regeneration device;
(2) calculating the alkali liquor flow required by the air discharged under different working conditions to reach an emission threshold according to the alkali liquor selected in the step (1), selecting the maximum working condition flow and considering a certain margin to serve as calculation basis of equipment, internal parts, pipelines and the like;
(3) calculating the tower diameter of the alkali liquor absorption tower, the type and the size and the structural type of the washing alkali liquor distributor according to the alkali liquor, the alkali liquor consumption and the treatment gas amount determined in the step (1) and the step (2);
(4) determining the required amount of the alkali liquor in a single period according to the alkali liquor conveying mode, the regeneration period and the alkali liquor consumption of the device, and taking a certain design allowance as a calculation basis of the alkali liquor storage tank on the basis, thereby determining the equipment size of the liquid storage tank;
(5) and (4) according to the sizes and the structural types of the alkali liquor absorption tower and the storage tank designed in the steps (3) and (4), equipment arrangement and pipeline arrangement are carried out, the calculation of the process parameters such as the lift and the flow of the circulating pump is completed by combining the arrangement condition and the alkali liquor using amount, and the alkali washing circulating pump with appropriate flow, lift and material is selected by combining the alkali liquor property.
Preferably, in the step (1), the alkali solution is one of a NaOH solution, a MDEA solution and ammonia water.
Preferably, in the step (3), the structural form of the lye absorption tower can be a plate tower or a packed tower or a tower of a combination of a plate and a packed tower; the structural form of the alkali liquor absorption tower is selected according to whether main components in the sulfur-rich liquid can be crystallized to block internal parts under operating conditions, ammonium bicarbonate crystals are easily generated when ammonia liquid is used as alkali wash liquid, and the structural form of the alkali liquor absorption tower adopts a plate tower.
Preferably, in step (3), the crystallization is easily caused, and a heat source such as steam, hot water, etc. may be used for the heating treatment.
In the invention, in the step (4), the consumption of the alkali liquor is the consumption of the alkali liquor after the crystallization of the alkali liquor reaches the saturation degree.
In the step (1), the temperature of the discharged air is 50-80 ℃, the pressure is 0-0.2 MPaG, and H in the discharged air2The S content is 0.1 (V)% -25 (V)%.
Compared with the prior art, the invention has the advantages that: the invention effectively removes H in the exhaust gas of the vacuum pump by washing with alkali liquor2S, the problem of peculiar smell of the exhaust gas is eliminated, and the field operation environment is improved; the method has the advantages of simple process flow, less added equipment, lower investment and operation cost, small system pressure drop, no need of higher pressure of the exhaust gas, no need of additionally adding a control scheme, small equipment occupation area and higher flexibility.
Drawings
FIG. 1 is a process flow diagram of an embodiment of the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1, the process system adopted by the coal gasification vent gas odor removal process of the embodiment includes:
the vacuum flash evaporation separation tank 1 is provided with an input port for inputting vacuum flash evaporation gas 101, the top of the vacuum flash evaporation separation tank is provided with an air outlet for outputting flash evaporation gas 103, and the bottom of the vacuum flash evaporation separation tank is provided with a liquid outlet for discharging condensate 102;
the vacuum pump 2 is arranged at the air outlet of the vacuum flash separation tank 1;
the vacuum pump separation tank 3 is provided with an inlet for inputting flash evaporation gas 103 output from the top of the vacuum flash evaporation separation tank 1, an outlet for outputting exhaust gas 106 of the vacuum pump separation tank is arranged at the top, and a liquid outlet for discharging condensate 105 is arranged at the bottom;
an alkali liquor absorption tower 4 arranged at the downstream of the vacuum pump separation tank 3 and provided with an input port for inputting the exhaust gas 106 of the vacuum pump separation tank, an output port for outputting qualified exhaust gas 109 at the top and rich H at the bottom2S a liquid outlet for inputting alkali liquor 108;
an alkali liquor storage tank 6 with a supply of rich H2An inlet for inputting S alkali liquor 108, the top of the inlet is provided with a device capable of introducing H2The discharge port and the bottom of the S from the air discharge to the safe place are connected withA pipeline for the alkali liquor 107 to flow back from the upper part of the alkali liquor absorption tower 4, wherein the pipeline is provided with an alkali liquor circulating pump 5, and the pipeline is provided with a valve; fresh alkali liquor 110 can be introduced into the alkali liquor storage tank 6, and spent rich alkali liquor or waste alkali liquor 111 can be discharged from a pipeline.
The process method of the embodiment comprises the following steps:
(1) according to the temperature, pressure, flow and H of the vent gas2The S content, the most suitable washing alkali liquor is determined by combining the configuration condition of alkali liquor used by available process devices or other auxiliary facilities in the device area and the configuration condition of a concentrated rich liquor regeneration device;
(2) calculating the alkali liquor flow required by the air discharged under different working conditions to reach an emission threshold according to the alkali liquor selected in the step (1), selecting the maximum working condition flow and considering a certain margin to serve as calculation basis of equipment, internal parts, pipelines and the like;
(3) calculating the tower diameter of the alkali liquor absorption tower, the type and the size and the structural type of the washing alkali liquor distributor according to the alkali liquor, the alkali liquor consumption and the treatment gas amount determined in the step (1) and the step (2);
(4) determining the required amount of the alkali liquor in a single period according to the alkali liquor conveying mode, the regeneration period and the alkali liquor consumption of the device, and taking a certain design allowance as a calculation basis of the alkali liquor storage tank on the basis, thereby determining the equipment size of the liquid storage tank;
(5) and (4) according to the sizes and the structural types of the alkali liquor absorption tower and the storage tank designed in the steps (3) and (4), equipment arrangement and pipeline arrangement are carried out, the calculation of the process parameters such as the lift and the flow of the circulating pump is completed by combining the arrangement condition and the alkali liquor using amount, and the alkali washing circulating pump with appropriate flow, lift and material is selected by combining the alkali liquor property.
In the step (1), the alkali liquor is one of NaOH solution, MDEA solution and ammonia water.
In the step (3), the structural type of the alkali liquor absorption tower 4 can be a plate tower or a packed tower or a tower with a combination type of tower plates and packing; the structural type of the alkali liquor absorption tower 4 is selected according to whether the main components in the sulfur-rich liquid can be crystallized to block the separation internal parts under the operation condition, ammonium bicarbonate crystals are easily generated when ammonia liquid is used as alkali wash liquid, and the structural type of the alkali liquor absorption tower adopts a plate tower.
In the step (3), the crystallization is easy, and a heat source such as steam, hot water and the like can be used for heating treatment.
In this embodiment, in the step (4), the consumption of the lye is the consumption of the lye after the lye crystals reach saturation.
In the step (1), the temperature of the discharged air is 50-80 ℃, the pressure is 0-0.2 MPaG, and the H in the discharged air2The S content is 0.1 (V)% -25 (V)%.
The process of the present embodiment is described below with specific working conditions. The parameters of the exhaust gas 106 discharged from the vacuum pump separation tank 3 are shown in table 1.
TABLE 1 gas composition of the vacuum pump separation tank vent gas
Figure BDA0002747703820000041
When the alkali liquor is MDEA solution, the process of this example is as follows:
(1) the exhaust gas from the top of the vacuum pump separation tank 3 with the pressure of 0.02MPaG and the temperature of 78 ℃ enters the alkali liquor absorption tower 4 through a pipeline, and the flow rate is about: 1.3m3H is used as the reference value. After being uniformly distributed by a gas phase distributor, the mixture rises in the tower;
(2) the alkali liquor absorption tower 4 is internally provided with 3m Raschig ring packing, the exhaust gas is in reverse contact with the MDEA solution sprayed from the upper part in the packing layer, the exhaust gas is discharged into the atmosphere from the pipe orifice of the tower top after contact absorption, and the composition of the treated exhaust gas is detailed in a table 2;
TABLE 2 alkali absorption column vent gas H2Concentration of S
Working conditions Initial exhaust gas H2Concentration of S Initial exhaust gas H2Concentration of S
Design conditions <10ppm <30ppm
Checking the operating conditions <10ppm <30ppm
Actual coal type <30ppm <60ppm
High sulfur coal <50ppm <100ppm
(3) Absorb H2S、CO2The MDEA-rich solution with the same acid gas flows back to the alkali liquor storage tank 6 from a bottom pipe opening by using potential difference for recycling, the size of the storage tank is 1600 multiplied by 2000(mm), and the effective volume is 4m3；
(4) MDEA in the alkali liquor storage tank 6 is pumped back to the alkali liquor absorption tower 4 for exhaust gas washing through a newly added MDEA circulating pump, wherein the circulating amount of the MDEA solution is 2m3/h；
(5) When the usage time of the MDEA solution reaches the regeneration period, the MDEA solution is transported back to the regeneration device through a tank car for regeneration, and the regeneration period of the MDEA solution is shown in the table 3 according to different gasified coal types.
TABLE 3 MDEA regeneration period under different coal types
Design conditions Checking the operating conditions Actual coal type High sulfur coal
Dry basis sulfur content/wt% 0.67 0.67 1.1 4.3
Regeneration period/day of MDEA solution ～30 ～33 ～16 5～7
When the alkali solution is 20 wt% NaOH solution, the process of this example is as follows:
(1) the exhaust gas from the top of the vacuum pump separation tank with the pressure of 0.02MPaG and the temperature of 78 ℃ enters an alkali liquor absorption tower 4 through a pipeline, and the flow rate is about: 1.3m3H is used as the reference value. After being uniformly distributed by a gas phase distributor, the mixture rises in the tower;
(2) 3m Raschig ring packing is filled in the alkali liquor absorption tower 4, the exhaust gas is in reverse contact with NaOH solution sprayed from the upper part in the packing layer, and the exhaust gas is discharged into the atmosphere from the pipe orifice of the tower top after the contact absorption;
(3) absorb H2S、CO2The NaOH-rich solution of the acid gas flows back to the alkali liquor storage tank 6 for recycling by utilizing potential difference from the pipe orifice at the bottom of the tower;
(4) NaOH in the alkali liquor storage tank 6 is pumped back to the NaOH absorption tower through a newly added NaOH circulating pump to carry out exhaust gas washing, and the circulating amount of the NaOH solution is 2m3/h；
(5) When the service life of the NaOH solution reaches the regeneration period, the NaOH solution is transported back to the regeneration device through the tank car for regeneration, and the regeneration period of the NaOH solution is shown in the table 4 according to different gasified coal types.
TABLE 4 NaOH replacement cycle under different coal types
Design conditions Checking the operating conditions Actual coal type High sulfur coal
Dry basis sulfur content/wt% 0.67 0.67 1.1 4.3
Regeneration period/day of MDEA solution ～8 ～7 ～5 ～4.5

Claims (5)

1. A process for removing odor of coal gasification vent gas is characterized by comprising the following steps:
the adopted process system comprises
The vacuum flash evaporation separation tank is provided with an input port for inputting vacuum flash evaporation gas, the top of the vacuum flash evaporation separation tank is provided with an air outlet for outputting the flash evaporation gas, and the bottom of the vacuum flash evaporation separation tank is provided with a liquid outlet for discharging condensate;
the vacuum pump is arranged at the air outlet of the vacuum flash separation tank;
the vacuum pump separation tank is provided with an inlet for inputting flash steam output from the top of the vacuum flash separation tank, the top of the vacuum pump separation tank is provided with an outlet for outputting exhaust gas of the vacuum pump separation tank, and the bottom of the vacuum pump separation tank is provided with a liquid outlet for discharging condensate;
an alkali liquor absorption tower arranged at the downstream of the vacuum pump separation tank and provided with an input port for inputting the exhaust gas of the vacuum pump separation tank, an output port for outputting qualified exhaust gas at the top and a rich H supply at the bottom2A liquid outlet for inputting the S alkali liquor,
alkali liquor storage tank with supply of rich H2An inlet for inputting S alkali liquor, and an inlet at the top for inputting H2S, a discharge port which is emptied to a safe place, and the bottom of the discharge port are connected with a pipeline for alkali liquor to flow back from the upper part of the alkali liquor absorption tower, and an alkali liquor circulating pump is arranged on the pipeline;
the process method comprises
(1) According to the temperature, pressure, flow and H of the vent gas2The S content, the most suitable washing alkali liquor is determined by combining the configuration condition of alkali liquor used by available process devices or other auxiliary facilities in the device area and the configuration condition of a concentrated rich liquor regeneration device;
(2) calculating the alkali liquor flow required by the air discharged under different working conditions to reach an emission threshold according to the alkali liquor selected in the step (1), selecting the maximum working condition flow and considering a certain margin to serve as calculation basis of equipment, internal parts, pipelines and the like;
(3) calculating the tower diameter of the alkali liquor absorption tower, the type and the size and the structural type of the washing alkali liquor distributor according to the alkali liquor, the alkali liquor consumption and the treatment gas amount determined in the step (1) and the step (2);
(4) determining the required amount of the alkali liquor in a single period according to the alkali liquor conveying mode, the regeneration period and the alkali liquor consumption of the device, and taking a certain design allowance as a calculation basis of the alkali liquor storage tank on the basis, thereby determining the equipment size of the liquid storage tank;
(5) and (4) according to the sizes and the structural types of the alkali liquor absorption tower and the storage tank designed in the steps (3) and (4), equipment arrangement and pipeline arrangement are carried out, the calculation of the process parameters such as the lift and the flow of the circulating pump is completed by combining the arrangement condition and the alkali liquor using amount, and the alkali washing circulating pump with appropriate flow, lift and material is selected by combining the alkali liquor property.
2. The coal gasification vent gas odor removal process according to claim 1, characterized in that: in the step (1), the alkali liquor is one of NaOH solution, MDEA solution and ammonia water.
3. The coal gasification vent gas odor removal process according to claim 1, characterized in that: in the step (3), the structural type of the alkali liquor absorption tower is selected according to whether main components in the sulfur-rich liquid can be crystallized to block internal parts under operating conditions, ammonium bicarbonate crystals are easily generated when ammonia liquid is used as alkali liquor, and the structural type of the alkali liquor absorption tower adopts a plate tower.
4. The coal gasification vent gas odor removal process according to claim 1, characterized in that: in the step (4), the consumption of the alkali liquor is the consumption of the alkali liquor after the crystallization of the alkali liquor reaches the saturation degree.
5. The coal gasification vent gas odor removal process according to claim 1, characterized in that: in the step (1), the temperature of the discharged air is 50-80 ℃, the pressure is 0-0.2 MPaG, and H in the discharged air2The S content is 0.1 (V)% -25 (V)%.
CN202011172404.0A 2020-10-28 2020-10-28 Process for removing peculiar smell of coal gasification vent gas Pending CN112480974A (en)

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CN207401338U (en) * 2017-09-30 2018-05-25 河南九龙环保有限公司 Circulation desulfurization system
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