CN214114973U - CO conversion condensate refining process system - Google Patents
CO conversion condensate refining process system Download PDFInfo
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- CN214114973U CN214114973U CN202022806725.3U CN202022806725U CN214114973U CN 214114973 U CN214114973 U CN 214114973U CN 202022806725 U CN202022806725 U CN 202022806725U CN 214114973 U CN214114973 U CN 214114973U
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Abstract
The utility model provides a CO transform condensate refines process systems, including high temperature condensate strip tower, low temperature condensate strip tower, stripping gas knockout tower and carbon dioxide strip tower, high temperature condensate strip tower top has connected gradually used heat boiler and vapour and liquid separator to be connected with low temperature condensate strip tower, low temperature condensate strip tower passes through the water-cooling pipeline and is connected with stripping gas knockout tower, passes through the pipeline at the bottom of the stripping gas knockout tower and is connected with washing water heater, and washing water heater passes through the pipeline and is connected with carbon dioxide strip tower. CO transform condensate refined process systems pass through four tower lime set, reduce the corruption of gasification water system, rationally retrieved the height and dodged the effective gas composition in the gas and the transform condensate, retrieve the ammonia in the stripping gas, guarantee the long-term steady operation of device.
Description
Technical Field
The utility model belongs to the technical field of coal chemical industry and equipment, especially, relate to a CO transform condensate refines process systems.
Background
The condensate stripping device mainly uses gasified high flash gas and low-pressure steam as heat sources to purify high-temperature conversion condensate and low-temperature conversion condensate generated by the CO conversion device and remove H contained in condensate2S、NH3And CO and the like are sent back to the gasification device to be used as water supplement of the gasification device, so that the supplement of desalted water of the gasification device is reduced.
The common low-temperature shift condensate treatment process comprises a single-tower steam stripping process and a two-tower steam stripping process, wherein the specific processes are respectively as follows:
single-column stripping flow: the low-temperature condensate from the ammonia washing tower of the conversion section is decompressed to 0.5MPa through a pressure regulating valve and enters the top of a low-temperature condensate stripping tower, flash steam at the top of a high-temperature condensate flash evaporation tank enters the middle of the stripping tower to serve as a supplementary heating medium, gasified high-flash steam and low-pressure steam serve as main stripping heating media, the operating pressure of the low-temperature condensate stripping tower is 0.24MPa, overhead stripping gas (0.24MPa and 120 ℃) is cooled to 75 ℃ through a water cooler and enters a gravity type gas-liquid separation tank to be subjected to gas-liquid separation, the gas phase is sent to a sulfur recovery device through reheating at 15-30 ℃, and the liquid phase can be selectively refluxed to the stripping tower or sent to the outside for sewage treatment. The condensate (0.24MPa, 130 ℃) at the bottom of the low-temperature condensate stripping tower is pressurized to 2.0MPa by a pump and then is sent back to a deaerator of a gasification device.
Publication (bulletin) No.: CN104495965A discloses a double-tower stripping process, which is provided with CO2Stripping column and NH3Rectification column, CO2Acid gas stripped by the stripping tower is sent to a sulfur recovery unit, and NH is added3A stripping section and a rectifying section of the refining tower, wherein the stripping section is used for extracting CO2And (4) preparing rich ammonia gas or ammonia water in the rectifying section of ammonia in the liquid of the stripping tower.
The traditional condensate treatment process in the CO conversion section generally has the following problems:
1) the high-temperature condensate is simple to treat, and the high-temperature condensate returned to gasification contains high acid gas components, so that the corrosion of a process water system of a gasification device is aggravated;
2) stripping tower outlet mouth H of low-temperature condensate single-tower stripping process2S、NH3、CO2The medium is easy to form ammonium bicarbonate crystals at low temperature, and a pipeline valve is blocked, so that the steam stripping device is stopped;
3) the stripping gas at the outlet of the stripping tower contains CO and H2Directly sent into a sulfur recovery device for treatment, thereby causing the waste of products;
4) the feed of the double-tower process ammonia refining tower is CO2The condensate at the bottom of the stripping tower has large tower load, high equipment investment and lower purity of the refined rich ammonia gas or ammonia water.
Disclosure of Invention
In view of this, the utility model aims at providing a CO transformation condensate refines processing system adopts four tower condensate devices to refine the high temperature condensate to overcome prior art's defect.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this: a CO conversion condensate refining process system comprises a high-temperature condensate stripping tower, a low-temperature condensate stripping tower, a stripping gas separation tower and a carbon dioxide stripping tower, wherein the top of the high-temperature condensate stripping tower is sequentially connected with a waste heat boiler and a gas-liquid separator through pipelines, a top extraction opening and a bottom extraction opening of the gas-liquid separator are respectively connected with a middle extraction opening of a tower body of the low-temperature condensate stripping tower through pipelines, and the bottom of the high-temperature condensate stripping tower is connected with a condensate pump through a pipeline;
the top extraction outlet of the low-temperature condensate stripping tower is connected with the extraction inlet at one side of the bottom of the stripping gas separation tower through a water cooling pipeline, the water cooling pipeline is connected with a water cooler, and the bottom extraction outlet of the low-temperature condensate stripping tower is connected with a washing water heater through a pipeline;
the bottom of the stripping gas separation tower is connected with a washing water heater through a pipeline, and the washing water heater is connected with a sampling port in the middle of the carbon dioxide stripping tower through a pipeline;
the bottom extraction outlet of the carbon dioxide stripping tower is divided into two branches, one branch is connected with an ammonia refining device, the other branch is connected with a reboiler, and the reboiler is connected to one side of the bottom of the carbon dioxide stripping tower through a return line.
The high-temperature condensate flash tank comprises a high-temperature condensate flash tank body, a high-temperature condensate input pipeline, a high-temperature condensate flash tank top mining outlet, a high-temperature condensate stripper, a high-temperature condensate flash tank bottom mining outlet, a hydraulic turbine, two branch circuits, one branch circuit and the other branch circuit, wherein the high-temperature condensate input pipeline is connected to one side of the high-temperature condensate flash tank body, the mining outlet at the top of the high-temperature condensate flash tank is connected with one side of the bottom of the high-temperature condensate stripper through a pipeline, the mining outlet at the bottom of the high-temperature condensate flash tank is connected with the hydraulic turbine through a pipeline, the hydraulic turbine is connected with the two branch circuits, one branch circuit is connected with one side of the top of the high-temperature condensate stripper, and the other branch circuit is connected with a condensate pump.
Wherein a gas extraction pipeline is connected with an extraction outlet at the top of the stripping gas separation tower;
one sides of the tops of the stripping gas separation tower and the carbon dioxide stripping tower are respectively connected with a washing water input pipeline;
the top extraction outlet of the carbon dioxide stripping tower is connected with an acid gas extraction pipeline.
Wherein, one side of the tower bottom of the high-temperature condensate stripping tower and one side of the tower bottom of the low-temperature condensate stripping tower are respectively connected with a steam input pipeline;
one side of the bottom of the high-temperature condensate stripping tower is also connected with a high flash gas input pipeline;
one side of the top of the low-temperature condensate stripping tower is connected with a low-temperature condensate input pipeline.
The CO conversion condensate refining process method comprises the following steps: the high-temperature conversion condensate enters a high-temperature condensate flash tank to be subjected to flash evaporation separation to give two gas-liquid phases, the flash evaporation gas phase and the gasified high-flash gas are jointly used as a heat source of a high-temperature condensate stripping tower, the flash evaporation liquid phase is subjected to energy recovery by a hydraulic turbine and is used for driving a condensate pump, and the low-pressure condensate formed by the flash evaporation liquid phase passing through the hydraulic turbine enters the high-temperature condensate tower to be stripped;
purified high-temperature condensate at the bottom of the high-temperature condensate tower is pumped to a gasification device for recycling through a condensate pump driven by a hydraulic turbine, and stripping gas at the top of the tower enters a waste heat boiler to recover heat from boiler water in the waste heat boiler and generate steam as a byproduct;
the method comprises the following steps that stripping gas and condensate at the outlet of a waste heat boiler enter a gas-liquid separator for gas-liquid separation, gas phase and liquid phase in the gas-liquid separator enter the middle part of a low-temperature condensate stripping tower, and low-temperature conversion condensate enters the upper part of the low-temperature condensate stripping tower;
cooling the overhead stripping gas of the low-temperature condensate stripping tower in a water cooler, then feeding the cooled overhead stripping gas into a stripping gas separation tower to be sprayed and washed by washing water, recycling the washed gas phase rich in carbon monoxide and hydrogen as a raw material of a conversion device, and feeding the bottom condensate of the low-temperature condensate stripping tower into a gasification device for recycling;
the liquid phase at the bottom of the stripping gas separation tower is divided into two parts, one part of cold feed enters a second layer of filler of the carbon dioxide stripping tower, and the other part of cold feed enters the carbon dioxide stripping tower from a first layer of tower plate after being heated by condensate at the bottom of the low-temperature condensate stripping tower;
the acid gas at the top of the carbon dioxide stripping tower is sent into a sulfur recovery device, the dilute ammonia water at the bottom of the tower is divided into two streams, one stream enters an ammonia refining device to recover liquid ammonia, and the other stream flows back to the carbon dioxide stripping tower after being evaporated by a reboiler.
The low-pressure steam is used as a heat source and enters from the bottoms of the high-temperature condensate stripping tower and the low-temperature condensate stripping tower respectively;
the stripping pressure of the high-temperature condensate stripping tower is 0.8-1.0MPa, and the tower top temperature is 160-180 ℃;
the operation pressure of the low-temperature condensate stripping tower is 0.3-0.5MPa, and the tower top temperature is 115-135 ℃;
the high-temperature condensate stripping tower and the low-temperature condensate stripping tower both adopt plate towers, and the number of the tower plates is 8-18.
Wherein the washing water enters from one side of the top of the stripping gas separation tower and the carbon dioxide stripping tower respectively; the stripping gas separation tower and the carbon dioxide stripping tower utilize the heat of the purified water to heat the washing condensate to 130-150 ℃;
the stripping gas separation tower adopts a plate tower, the number of tower plates is 8-18 layers, the operating pressure of the stripping gas separation tower is 0.2-0.4MPa, the tower top temperature is 115-135 ℃, and the tower bottom temperature is 30-45 ℃;
the upper part of the carbon dioxide separation tower adopts packing, the lower part adopts a tower plate, the operating pressure of the carbon dioxide stripping tower is 0.2-0.4MPa, and the tower top temperature is 115-135 ℃.
Wherein the pressure of the high-temperature condensate flash tank is controlled to be 3.6-5.6MPa, and the operation temperature is 160-195 ℃.
Wherein the gas-liquid separation tank adopts a gas-liquid separator or a high-efficiency separator with a wire mesh demister;
the operation pressure of the gas-liquid separation tank is 0.75-0.95 MPa.
Wherein the pressure of the high-temperature condensate at the outlet of the hydraulic turbine is 0.8-1.0 MPa;
the water cooler adopts a graphite heat exchanger; the temperature of a stripping gas outlet of the water cooler is 30-45 ℃;
the waste heat boiler adopts a kettle type waste heat boiler for energy recovery, and a byproduct of 0.35-0.45MPa saturated steam is obtained.
Waste heat boiler, washing water heater, water cooler, reboiler be heat exchanger, it includes two heat transfer passageways respectively, a heat transfer passageway is the tube side, another heat transfer passageway is the shell side.
Compared with the prior art, the CO conversion condensate refining process system has the following advantages:
(1) a CO transform condensate refined process systems, through four tower condensate devices, reduce the corruption of gasification water system, rationally retrieved the effective gas composition (CO and H) that gasifies the high flash of gas and transform the condensate2) Recovering ammonia from the stripping gas; the long-term stable operation of the device is ensured, and the production cost of enterprises is saved.
(2) The utility model discloses a CO transform condensate refining process system, adopt high temperature condensate steam stripping technology, the high temperature condensate has deeply purified, has reduced the acid gas composition in the high temperature condensate of returning gasification, has reduced the corruption of gasification equipment process water system;
(3) the utility model discloses a CO transformation condensate refining process system, adopted high temperature condensate steam stripping technology, the heat source is high temperature condensate flash tank top flash steam and gasification high flash gas, need not extra steam input when high temperature condensate steam stripping tower normally operates, energy saving;
(4) the utility model discloses a CO conversion condensate refining process system, adopt hydraulic turbine to retrieve the pressure energy of condensate in the high temperature condensate flash tank, provide the energy for the operation of condensate pump, reduced the energy consumption of device;
(5) the utility model discloses a CO conversion condensate refining process system, which utilizes the heat of the stripping gas to produce low-pressure saturated steam as a byproduct, and effectively utilizes low-level heat;
(6) a CO transform condensate refining process system, utilize the flash distillation vapour on the top of the stripping gas knockout tower and stripping gas knockout tower to retrieve effective gas (CO and H)2) The economic benefit is improved;
(7) a CO transform condensate refining process system utilizes CO2The separating tower and the ammonia refining device separate ammonia from acid gas, solve the problem that an acid gas pipeline is blocked by ammonium bicarbonate crystallization, prepare liquid ammonia and ammonia water according to the requirement by the recycled ammonia, obtain the ammonia water with the purity higher than 99 percent, reduce the emission of the acid gas, protect the process and have strong operation reliability.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without undue limitation.
In the drawings:
FIG. 1 is a schematic flow chart of a CO shift condensate refining process according to an embodiment of the present invention;
fig. 2 is a schematic flow diagram of a CO single-column stripping process according to a comparative example of the present invention.
Description of reference numerals:
c-01, a high-temperature condensate stripping tower; c-02, low-temperature condensate stripping tower; c-03, a stripping gas separation tower; c-04, a carbon dioxide stripping tower; d-01, a gas-liquid separator; e-01, a waste heat boiler; e-02, a water cooler; e-03, a washing water heater; e-04, a reboiler; HT-01, hydraulic turbine; p-01, a condensate pump; v-01, a high-temperature condensate flash tank;
c' -02, low-temperature condensate stripper; d' -01, a gas-liquid separator; e' -01 and a water cooler; e' -02, a superheater; v' -01, a high-temperature condensate flash tank; p' -01 and a condensate pump.
Detailed Description
For a better understanding of the present invention, reference will now be made in detail to the present invention as illustrated in the accompanying drawings. In order to illustrate the present invention in detail, the following examples illustrate details of the process and are not intended to unduly limit the invention.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
Examples
As shown in FIG. 1, the condensate (H as feed) is converted at high temperature2、CO、H2O、H2S, wherein 99% is H2O) enters a high-temperature condensate flash tank V-01 through a high-temperature condensate input pipeline to carry out flash separation on gas-liquid two phases, a top extraction port of the high-temperature condensate flash tank (V-01) is connected with one side of the bottom of the high-temperature condensate stripping tower C-01 through a pipeline, the pressure of the high-temperature condensate flash tank V-01 is controlled to be 3.6-5.6MPa, the operation temperature is 160-195 ℃, the flash vapor phase is extracted from the top of the high-temperature condensate flash tank V-01, the gas-phase components account for 1-5% of the total amount of the components, and the flash vapor phase and the gasified high-flash gas enter the bottom of the high-temperature condensate stripping tower C-01 through a pipeline and are jointly used as a heat source of the high-temperature condensate stripping tower C-01; the temperature of the high flash gas from gasification is 170-190 ℃, so that no additional steam input source is needed during normal operation of the high-temperature condensed gas tower C-01, the energy input is saved, the gasification water quality is improved, and the corrosion of a gasification water system is reduced.
And a flash liquid phase is extracted from a bottom extraction outlet of the high-temperature condensate flash tank V-01, the liquid phase component accounts for 95-99% of the total amount of the components, the energy of the flash liquid phase is recovered through a hydraulic turbine HT-01 and is used for driving a condensate pump P-01, and the low-pressure condensate formed by the flash liquid phase through the hydraulic turbine HT-01 is extracted from one side of the top of the high-temperature condensate stripping tower C-01 through a pipeline.
8-18 layers of tower plates are arranged in the high-temperature condensate stripping tower C-01, the stripping pressure of the high-temperature condensate stripping tower is 0.8-1.0MPa, the gas phase temperature at the top of the tower is 160-180 ℃, gas phase components are extracted from the top of the high-temperature condensate stripping tower C-01, and purified high-temperature condensate at the bottom of the high-temperature condensate stripping tower C-01 is sent to a condensate pump P-01 driven by a hydraulic turbine HT-01The gasification device is recycled, liquid phase components at the bottom of the high-temperature condensate stripping tower C-01 enter a condensate pump P-01 for condensation cooling, the energy of the condensation cooling comes from a hydraulic turbine HT-01, the pressure of the high-temperature condensate at the outlet of the hydraulic turbine HT-01 is 0.8-1.0MPa, the hydraulic turbine HT-01 recovers the pressure energy in the high-temperature condensate, the pressure energy in the high-temperature condensate is converted into mechanical energy for driving the high-temperature condensate pump P-01, the energy of the high-temperature condensate is recovered by the hydraulic turbine HT-01, the energy consumption of the device is reduced, and the condensate pump P-01 recovers NH in the high-temperature condensate stripping tower C-013、H2、CO、CO2And (4) gasifying the condensate of the acidic gas to obtain pure water.
One side of the bottom of the high-temperature condensate stripping tower C-01 is connected with a steam input pipeline which provides steam for the high-temperature condensate stripping tower C-01 when the system is started, and the steam does not need to be provided when the system is normally operated after the system is started.
The steam stripping gas extracted from the top of the high-temperature condensate stripping tower C-01 enters a tube pass of a waste heat boiler E-01 through a pipeline for heat exchange, the steam stripping gas in the tube pass is high in temperature, the shell pass of the waste heat boiler E-01 is supplied with water by a boiler, the water in the shell pass is low in temperature and exchanges heat with the steam stripping gas in the tube pass of the waste heat boiler E-01, the steam byproduct is extracted after the water in the shell pass is heated, 0.35-0.45MPa saturated steam is produced, and the steam stripping gas in the tube pass and the condensate after the temperature is reduced enter a gas-liquid separator D-01 for gas-liquid separation.
The gas-liquid separator D-01 adopts a gas-liquid separator or a high-efficiency separator with a wire mesh demister, the operating pressure is 0.75-0.95MPa, gas-phase components are extracted from the top of the gas-liquid separator D-01, the gas-phase components enter the middle part of the low-temperature condensate stripping tower C-02 through a pipeline, and the gas-phase components and low-pressure steam are jointly used as a heat source of the low-temperature condensate stripping tower C-02; and low-temperature transformation condensate is extracted from the bottom of the gas-liquid separator D-01 and enters the upper part of the low-temperature condensate stripping tower C-02 through a pipeline for stripping.
The low-temperature conversion condensate is collected from one side of the top of a low-temperature condensate stripping tower C-02 through a pipeline, the low-temperature condensate is extracted from the components in a gas-liquid separation tank D-01, the low-temperature condensate stripping tower C-02 adopts a plate tower, the number of tower plates is 8-18, the operating pressure is 0.3-0.5MPa, the temperature of the top of the tower is 120-, the temperature of circulating water in the shell pass of the water cooler E-02 is low, the circulating water exchanges heat with stripping gas in the tube pass of the water cooler E-02, and the stripping gas in the tube pass of the water cooler E-02 is cooled and enters one side of the bottom of the stripping gas separation tower C-03 through a pipeline to be stripped;
the inlet temperature of the stripping gas separation tower C-03 is 30-45 ℃, one side of the top of the stripping gas separation tower C-03 is connected with a washing water input pipeline, washing water enters the stripping gas separation tower C-03, the washing condensate is heated to 130-150 ℃ by utilizing the heat of purified water, and a gas phase component (H) is extracted from the top of the stripping gas separation tower C-03 after washing by the washing water2、CO、CO2) Gas phase component (H)2、CO、CO2) The flash steam is returned to transform after being extracted through a gas extraction pipeline, and effective components are recovered to be used as raw materials of a transform inlet.
The temperature of the tower bottom is 120-130 ℃, the tower bottom produced liquid phase component of the low-temperature condensate stripping tower C-02 enters a pipe pass of the washing water heater-03 through a pipeline, and the tower bottom produced liquid phase component (NH) of the stripping gas separation tower C-033、H2S) is divided into two parts, one part of cold feed enters a second layer of filler of a carbon dioxide stripping tower C-04, the other part of cold feed enters the carbon dioxide stripping tower C-04 from a first layer of tower plate after being heated by condensate at the bottom of a low-temperature condensate stripping tower C-02, and a liquid phase component (NH) at the bottom of a stripping gas separation tower C-033、H2S) enters a shell side of a washing water heater E-03 through a pipeline, exchanges heat with a liquid-phase component at the bottom of a low-temperature condensate stripping tower C-02, and directly gasifies a condensate after the liquid-phase component extracted at the bottom of the low-temperature condensate stripping tower C-02 exchanges heat and is cooledAnd (6) extracting.
Heating condensate at the bottom of a low-temperature condensate stripping tower C-02, feeding the condensate into a carbon dioxide stripping tower C-04 from a first-layer tower plate, feeding filler into a carbon dioxide separation tower C-04 from the upper part, feeding tower plates from the lower part, heating the condensate to 130-150 ℃ by using the heat of purified water, washing the condensate by using the washing water, and collecting an acidic gas CO from the top of the carbon dioxide stripping tower C-042And H2S, acid gas CO2And H2S enters a sulfur recovery device through a pipeline for further desulfurization recovery; dilute ammonia water is extracted from the bottom of the carbon dioxide stripping tower C-04, the diluted ammonia water is extracted from the bottom of the tower and divided into two streams, one stream enters an ammonia refining device through a pipeline for liquid ammonia recovery to obtain ammonia water with the purity higher than 99%, emission of acid gas is reduced, and the other stream is evaporated by a reboiler E-04 and then flows back to one side of the bottom of the carbon dioxide stripping tower C-04 to continue circulation.
A certain chemical plant adopts a CO conversion condensate refining process to treat 600t/h of high-temperature conversion condensate and 150t/h of low-temperature conversion condensate, the liquid ammonia content of the low-temperature conversion condensate is 2000ppm, the gasified high flash gas is 60t/h, and the content of each component is shown in table 1:
TABLE 1
Adopt CO transform condensate refining process systems, H in high temperature condensate2S content < 20ppm, NH3The content is less than 80ppm, and effective gases (CO and H) are recovered2)1900Nm3The flow of acid gas sent to a sulfur recovery device is 1050kg/h, wherein the flow of the recovered liquid ammonia is 345kg/h, the flow of the byproduct steam is 50t/h (which is equivalent to saving 1.2t/h of raw material coal).
Comparative example
As shown in FIG. 2, FIG. 2 shows a process flow of CO single-column stripping, high-temperature shift condensate (material is H)2、CO、H2O、H2S, it99% of the total are H2O) enters a high-temperature condensate flash tank V '-01 through a pipeline through high-temperature conversion condensate, the high-temperature condensate flash tank V' -01 carries out flash separation on the high-temperature conversion condensate to obtain two gas-liquid phases, a top extraction port of the high-temperature condensate flash tank V '-01 is connected with one side of the bottom of a low-temperature condensate stripping tower C' -02 through a pipeline, the pressure of the high-temperature condensate flash tank V '-01 is controlled to be 3.6-5.6MPa, the operation temperature is 160-195 ℃, a flash vapor phase is extracted from the top of the high-temperature condensate flash tank V' -01, gas-phase components account for 1-5% of the total weight of the components, and the flash vapor phase and gasified high-flash gas enter the bottom of the low-temperature condensate stripping tower C '-02 through pipelines and are jointly used as a heat source for supplementing the low-temperature condensate C' -02; the temperature of the high flash gas from gasification is 170-190 ℃. One side of the bottom of the low-temperature condensate stripping tower C '-02 is connected with a steam input pipeline, and steam is provided for the low-temperature condensate stripping tower C' -02 when the system normally operates.
And a flash liquid phase is extracted from a bottom extraction outlet of the high-temperature condensate flash tank V '-01, the liquid phase component accounts for 95-99% of the total amount of the components, and the flash liquid phase is recycled by a condensate pump P' -01 pressurizing and conveying gasification device.
The low-temperature conversion condensate is collected from one side of the top of a low-temperature condensate stripping tower C ' -02 through a pipeline, the low-temperature condensate stripping tower C ' -02 adopts a plate tower, the number of tower plates is 8-20, the operating pressure is 0.3-0.5MPa, the temperature of the top of the tower is 120-150 ℃, stripping gas is collected from the top of the low-temperature condensate stripping tower C ' -02, the stripping gas at the top of the low-temperature condensate stripping tower C ' -02 enters a water cooler E ' -01 through a pipeline for cooling, the water cooler E ' -01 adopts a metal shell-and-tube heat exchanger, the temperature of a stripping gas outlet of the water cooler E ' -01 is 65-85 ℃, the stripping gas collected from the top of the low-temperature condensate stripping tower C ' -01 enters a tube pass of the water cooler E ' -01, circulating water enters a shell pass of the water cooler E ' -01, and the temperature of the circulating water in the shell pass of the water cooler E ' -01 is lower, and the heat exchange is carried out between the condensed liquid and the stripping gas in the tube pass of the water cooler E ' -01, and the condensed liquid generated after the temperature of the stripping gas in the tube pass of the water cooler E ' -01 is reduced and the condensed liquid is introduced into a stripping gas separation tank D ' -01 through a pipeline for gas-liquid separation.
Gas-liquid separator D' -01 adopts a gas-liquid separator with a wire mesh demisterOr a high-efficiency separator with the operating pressure of 0.25-0.45MPa, gas-phase components are extracted from the top of the gas-liquid separator D '-01, the gas-phase components enter the acid gas superheater E' -02 through a pipeline to be heated and superheated, the superheater E '-02 adopts a metal shell-and-tube heat exchanger, the temperature of a steam stripping gas outlet of the superheater E' -02 is 90-95 ℃, the acid gas extracted from the top of the gas-liquid separator D '-01 enters the tube pass of the superheater E' -02, the steam enters the shell pass of the superheater E '-02, the temperature of the steam in the shell pass of the superheater E' -02 is high, the steam exchanges heat with the acid gas in the tube pass of the superheater E '-02, and after the temperature of the acid gas in the tube pass of the superheater E' -02 is raised, the acid gas (containing CO and H) is obtained2、NH3、CO2、H2S) entering a sulfur recovery device through a pipeline for sulfur recovery.
Liquid phase components extracted from the bottom of the gas-liquid separator D' -01 are sent to a sewage device for further treatment at the temperature of 65-85 ℃ and the ammonia concentration of about 2000-5000 ppm.
A certain chemical plant adopts the traditional high-temperature condensation flash evaporation and low-temperature condensation single-tower steam stripping process to treat 600t/h of high-temperature conversion condensate and 150t/h of low-temperature conversion condensate, the liquid ammonia content of the low-temperature conversion condensate is 2000ppm, the gasified high flash gas is 60t/h, and the contents of all components are shown in a table 2:
TABLE 2
Adopts the traditional high-temperature condensate flash evaporation and low-temperature condensate single-tower steam stripping process to remove H in the high-temperature condensate2S content 105ppm, NH3The content is 200ppm, no effective gas and liquid ammonia are recovered, no by-product steam is generated, the flow of acid gas sent to a sulfur recovery device is 3500kg/h, and the ammonia-containing sewage sent to a sewage device is about 3-5 t/h.
Comparison of investments
Taking the high-temperature conversion condensate of 600t/h and the low-temperature conversion condensate of 150t/h as an example, the single-tower steam stripping process is adopted, the equipment investment is about 2000 ten thousand, 3500kg/h of acid gas can be generated, the emission of waste gas of a factory is increased, high-concentration wastewater with ammonia concentration of more than 2.5 wt% is generated, and the wastewater treatment is difficult.
By adopting the CO conversion condensate refining process system of the utility model, the equipment investment is about 6500 ten thousand; CO and H can be recovered during equipment operation2And NH3The process system is free of high-concentration ammonia-containing sewage, does not need to additionally invest a sewage treatment device, generates less acid gas and is environment-friendly.
Principle of operation
The high-temperature condensate stripping tower C-01 extracts gas-phase components (CO and CO) under the action of high temperature2And H2) The acidic gas component in the high-temperature conversion condensate is reduced, the gasification water quality is improved, the corrosion of a gasification water system is reduced, the pressure energy in the high-temperature condensate is recovered through the hydraulic turbine HT-01, the pressure energy is converted into mechanical energy, the energy is provided for the operation of a condensate pump, and the energy consumption of the device is reduced; reasonably recovering effective gas components (CO and H) in gasified high-flash gas and conversion condensate2) The acidic gas at the top of the carbon dioxide stripping tower C-04 is extracted after being washed with washing water, and is subjected to desulphurization recovery; recovery of NH from acid gases3，The discharge amount of acid gas is reduced, the problem of crystallization blockage of an acid gas pipeline is avoided, the purity of the recovered liquid ammonia is higher than 99 percent, and low-level heat of the stripping gas is reasonably utilized to produce byproduct steam; the utility model discloses technology environment friendly saves the cost for the enterprise, improves economic benefits.
The above description is only a preferred embodiment of the present invention, and should not be taken as limiting the invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (4)
1. A CO conversion condensate refining process system is characterized in that: the device comprises a high-temperature condensate stripping tower (C-01), a low-temperature condensate stripping tower (C-02), a stripping gas separation tower (C-03), a high-temperature condensate flash tank (V-01) and a carbon dioxide stripping tower (C-04), wherein the top of the high-temperature condensate stripping tower (C-01) is sequentially connected with a waste heat boiler (E-01) and a gas-liquid separator (D-01) through pipelines, a top extraction port and a bottom extraction port of the gas-liquid separator (D-01) are respectively connected with an extraction port in the middle of a tower body of the low-temperature condensate stripping tower (C-02) through pipelines, and the bottom of the high-temperature condensate stripping tower (C-01) is connected with a condensate pump (P-01) through pipelines;
a tower top extraction outlet of the low-temperature condensate stripping tower (C-02) is connected with an extraction inlet at one side of the bottom of the stripping gas separation tower (C-03) through a water cooling pipeline, a water cooler (E-02) is connected on the water cooling pipeline, and a tower bottom extraction outlet of the low-temperature condensate stripping tower (C-02) is connected with a washing water heater (E-03) through a pipeline;
the bottom of the stripping gas separation tower (C-03) is connected with a washing water heater (E-03) through a pipeline, and the washing water heater (E-03) is connected with a middle sampling port of the carbon dioxide stripping tower (C-04) through a pipeline;
the bottom extraction port of the carbon dioxide stripping tower (C-04) is divided into two branches, one branch is connected with the ammonia refining device, the other branch is connected with the reboiler (E-04), and the reboiler (E-04) is connected to one side of the bottom of the carbon dioxide stripping tower (C-04) through a return line.
2. The CO shift condensate refining process system of claim 1, wherein: one side of a tank body of the high-temperature condensate flash tank (V-01) is connected with a high-temperature condensate input pipeline, a top extraction outlet of the high-temperature condensate flash tank (V-01) is connected with one side of the bottom of the high-temperature condensate stripping tower (C-01) through a pipeline, a bottom extraction outlet of the high-temperature condensate flash tank (V-01) is connected with a hydraulic turbine (HT-01) through a pipeline, the hydraulic turbine (HT-01) is connected with two branches, one branch is connected with one side of the top of the high-temperature condensate stripping tower (C-01), and the other branch is connected with a condensate pump (P-01).
3. The CO shift condensate refining process system of claim 1, wherein: a gas extraction pipeline is connected with an extraction outlet at the top of the stripping gas separation tower (C-03);
one sides of the top of the stripping gas separation tower (C-03) and the top of the carbon dioxide stripping tower (C-04) are respectively connected with a washing water input pipeline;
the top extraction outlet of the carbon dioxide stripping tower (C-04) is connected with an acid gas extraction pipeline.
4. The CO shift condensate refining process system of claim 1, wherein: one side of the bottom of each of the high-temperature condensate stripping tower (C-01) and the low-temperature condensate stripping tower (C-02) is connected with a steam input pipeline;
one side of the bottom of the high-temperature condensate stripping tower (C-01) is also connected with a high flash gas input pipeline;
one side of the tower top of the low-temperature condensate stripping tower (C-02) is connected with a low-temperature condensate input pipeline.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112520808A (en) * | 2020-11-26 | 2021-03-19 | 中国天辰工程有限公司 | CO conversion condensate refining process system and method |
| CN114921269A (en) * | 2022-06-09 | 2022-08-19 | 蒲城清洁能源化工有限责任公司 | Process for reducing ammonia nitrogen in methanol prepared from coal |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112520808A (en) * | 2020-11-26 | 2021-03-19 | 中国天辰工程有限公司 | CO conversion condensate refining process system and method |
| CN114921269A (en) * | 2022-06-09 | 2022-08-19 | 蒲城清洁能源化工有限责任公司 | Process for reducing ammonia nitrogen in methanol prepared from coal |
| CN114921269B (en) * | 2022-06-09 | 2023-10-27 | 蒲城清洁能源化工有限责任公司 | Ammonia nitrogen reducing process for coal-to-methanol |
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