AU2023296338A1 - Shift condensate treatment system and process - Google Patents
Shift condensate treatment system and process Download PDFInfo
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- AU2023296338A1 AU2023296338A1 AU2023296338A AU2023296338A AU2023296338A1 AU 2023296338 A1 AU2023296338 A1 AU 2023296338A1 AU 2023296338 A AU2023296338 A AU 2023296338A AU 2023296338 A AU2023296338 A AU 2023296338A AU 2023296338 A1 AU2023296338 A1 AU 2023296338A1
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- shift
- ammonia
- condensate
- pipeline
- ammonia water
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- 238000000034 method Methods 0.000 title claims abstract description 29
- 230000008569 process Effects 0.000 title claims abstract description 26
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 269
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 125
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 84
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 84
- 238000011084 recovery Methods 0.000 claims abstract description 68
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 46
- 230000023556 desulfurization Effects 0.000 claims abstract description 46
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 42
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 42
- 239000011593 sulfur Substances 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 27
- 239000007789 gas Substances 0.000 claims description 29
- 238000007670 refining Methods 0.000 claims description 25
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 22
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 15
- 238000002360 preparation method Methods 0.000 claims description 15
- 239000002253 acid Substances 0.000 claims description 14
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 13
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 13
- 239000001569 carbon dioxide Substances 0.000 claims description 11
- 238000000746 purification Methods 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 239000008213 purified water Substances 0.000 claims description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 abstract description 10
- 229910052921 ammonium sulfate Inorganic materials 0.000 abstract description 10
- 235000011130 ammonium sulphate Nutrition 0.000 abstract description 10
- 238000012423 maintenance Methods 0.000 abstract description 4
- 239000000126 substance Substances 0.000 abstract description 4
- 239000003245 coal Substances 0.000 abstract description 2
- 230000008901 benefit Effects 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- -1 iron ions Chemical class 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000006227 byproduct Substances 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910021645 metal ion Inorganic materials 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000011268 retreatment Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/022—Preparation of aqueous ammonia solutions, i.e. ammonia water
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/10—Separation of ammonia from ammonia liquors, e.g. gas liquors
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Physical Water Treatments (AREA)
Abstract
The present disclosure relates to the technical field of coal chemical industry, and in
particular to a shift condensate treatment system and process. The shift condensate treatment
system includes: at least two shift stripping towers and an ammonia recovery device. Inlets of
two of the shift stripping towers are respectively connected to shift low-temperature
condensate pipelines, and outlets are connected to a sulfur-containing low-concentration
ammonia water pipeline. The two shift low-temperature condensate pipelines are respectively
provided with a first pipeline connected to an inlet of the ammonia recovery device. The
sulfur-containing low-concentration ammonia water pipeline is provided with a second
pipeline connected to the inlet of the ammonia recovery device. An outlet of the ammonia
recovery device is connected to the sulfur-containing low-concentration ammonia water
pipeline through a third pipeline. The sulfur-containing low-concentration ammonia water
pipeline is configured to be connected to a boiler ammonia desulfurization apparatus. The
shift condensate treatment system solves the problems of water equilibrium and ammonia
equilibrium in a boiler desulfurization system, thereby improving quality of ammonium
sulfate; and also solves the problem that it is impossible to stop operation of a single shift
stripping tower for maintenance, thereby ensuring stable operation of the system.
16
Description
SHIFT CONDENSATE TREATMENT SYSTEM AND PROCESS The present disclosure claims the priority of Chinese patent application No.
202210842707.1, filed on July 18th, 2022 and entitled "SHIFT CONDENSATE
TREATMENT SYSTEM AND PROCESS", which is incorporated herein by reference in its
entirety.
The present disclosure relates to the technical field of coal chemical industry, and in particular to a shift condensate treatment system and process.
The information disclosed in this section is merely intended to promote the
understanding of the overall background of the present disclosure, and is not necessarily
taken as admitting or implying in any form that the information constitutes the prior art
already known to those of ordinary skill in the art.
A shift condensate refers to a low-temperature condensate and sulfur-containing
low-concentration ammonia water. The low-temperature condensate refers to the condensate, which is obtained when shift gas obtained after partial shift reaction of 215°C gasified water
gas, is cooled to 90°C or below during stage-by-stage cooling. This condensate contains
ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, iron ions, etc. The
sulfur-containing low-concentration ammonia water refers to sulfur-containing
low-concentration ammonia water produced by further performing steam stripping on the
low-temperature condensate through a shift stripping tower, gasifying the liquid phase,
condensing the gas phase and washing the condensate with demineralized water. This ammonia water contains H 2S, C02 , CO, H 2, iron ions, etc.
After the low-temperature condensate produced by condensation of shift system water
gas is stripped through the stripping tower and the gas phase is condensed and washed with
demineralized water, the low-concentration ammonia water is sent to a boiler flue gas
ammonia desulfurization system. The low-concentration ammonia water contains H2S, C02,
CO, 112, iron ions, etc., which affects the efficiency of flue gas desulfurization and the quality
of the byproduct ammonium sulfate, and destroys the ammonia equilibrium and water
equilibrium, causing excess and escape of ammonia. Moreover, when the shift stripping
towers treat the low-temperature condensate, the apparatus is poor in conditions and
frequently prone to corrosion and leakage, and it is impossible to stop operation of a single shift stripping tower for maintenance, which affects the long-term stable operation of the
system.
In view of the defects in the prior art, an objective of an embodiment of the present disclosure is to provide a shift condensate treatment system, so as to solve the problems of
water equilibrium and ammonia equilibrium in a boiler desulfurization system, thereby
improving quality of ammonium sulfate; and also solve the problem that it is impossible to
stop operation of a single shift stripping tower for maintenance, thereby ensuring stable
operation of the system. To achieve the foregoing objective, embodiments of the present disclosure use the
following technical solutions: A shift condensate treatment system includes: at least two shift stripping towers and an
ammonia recovery device. Inlets of two of the shift stripping towers are respectively
connected to shift low-temperature condensate pipelines, and outlets are connected to a
sulfur-containing low-concentration ammonia water pipeline. The two shift low-temperature
condensate pipelines are respectively provided with a first pipeline connected to an inlet of
the ammonia recovery device. The sulfur-containing low-concentration ammonia water
pipeline is provided with a second pipeline connected to the inlet of the ammonia recovery device. An outlet of the ammonia recovery device is connected to the sulfur-containing
low-concentration ammonia water pipeline through a third pipeline. The sulfur-containing
low-concentration ammonia water pipeline is configured to be connected to a boiler ammonia
desulfurization apparatus.
In another preferred implementation, the sulfur-containing low-concentration ammonia
water pipeline is provided with an ammonia water tower. A number of the shift stripping towers is three, and the outlets of the three shift stripping towers are all connected to the ammonia water tower.
In another preferred implementation, the ammonia recovery device includes a stripping
tower. The stripping tower has a shift condensate inlet in a middle, and the shift condensate inlet corresponds to the plurality of shift condensate pipelines. The stripping tower has an acid gas blow-down pipeline at a top, and a purified water discharge pipeline at a bottom.
In another preferred implementation, the ammonia recovery device further includes a three-stage partial condenser. A pipeline led out from the middle of the stripping tower is
connected to the three-stage partial condenser.
In another preferred implementation, the ammonia recovery device further includes a raw
water tank, and a bottom of the three-stage partial condenser is connected to the raw water
tank. In another preferred implementation, the ammonia recovery device further includes a
refining tower. An upper part of the three-stage partial condenser is connected to the refining tower. The refining tower is divided into an upper section and a lower section. At the lower
section, at least 95% of carbon dioxide and hydrogen sulfide are removed, and a solution is
used cyclically for absorption. At the upper section, fresh low-temperature concentrated
ammonia water is used to deeply remove the remaining carbon dioxide and hydrogen sulfide.
In another preferred implementation, the ammonia recovery device further includes an ammonia water preparation device. A pipeline led out of a top of the refining tower is
connected to the ammonia water preparation device, and the ammonia water preparation
device is configured to prepare ammonia water with different concentrations.
An embodiment of the present disclosure further provides a shift condensate treatment
process, including: converting a shift low-temperature condensate into sulfur-containing
low-concentration ammonia water by a shift stripping tower, the sulfur-containing
low-concentration ammonia water being used for ammonia desulfurization, and a number of the shift stripping towers being at least two; enabling, according an operating state, part or all
of the shift low-temperature condensate to enter an ammonia recovery device for purification
without passing through the shift stripping towers and then be used for the ammonia
desulfurization; and enabling, according to the operating state, part or all of the sulfur-containing low-concentration ammonia water to enter the ammonia recovery device for purification and then be used for the ammonia desulfurization.
In another preferred implementation, the purification in the ammonia recovery device
includes: after the shift condensate enters a stripping tower, rich ammonia gas in which part
of acid gases have been removed is drawn out from a middle of the stripping tower and then
sent to a three-stage partial condenser; in the three-stage partial condenser, the acid gases are
further removed, and crude ammonia gas is obtained from a top, which is sent to a refining tower; and in the refining tower, the acid gases are deeply removed.
In another preferred implementation, the refined ammonia gas in the refining tower is
sent into an ammonia water preparation device, and ammonia water prepared by the ammonia
water preparation device is used for boiler ammonia desulfurization or is sold.
One or more technical solutions provided in the embodiments of the present
disclosure has at least the following technical effects or advantages:
1. In the present disclosure, the stripping process based on shift stripping towers is used to treat the shift condensate. The number of the low-temperature condensate pipelines is
greater than that of the corresponding shift stripping tower pipelines, the corresponding
ammonia recovery process pipeline is added, and the plurality of shift low-temperature
condensate pipelines converge to the stripping tower of the ammonia recovery process,
thereby reducing the treatment amount of the shift stripping tower. When one of the shift
stripping towers breaks down, the low-temperature condensate may be treated by the
ammonia recovery device or the other shift stripping towers, which solves the problem that it is impossible to stop operation of a single shift stripping tower and improves the flexibility in
the operation of three parallel shift condensate systems. Thereby, there are many operation
modes to be selected, which reduces unnecessary start-up and shutdown costs and avoids
fluctuations of the system caused by start-up and shutdown for shift and heat recovery. The
sulfur-containing low-concentration ammonia water subjected to shift stripping and the
low-temperature condensate are mixed to the ammonia recovery device for treatment. After
the treatment, the high-purity ammonia is extracted and used for boiler ammonia desulfurization, which solves the problems of water equilibrium and ammonia equilibrium in
the boiler desulfurization system, improves the quality of the ammonium sulfate, and ensures the continuous and stable operation of the shift and heat recovery system and the boiler desulfurization system.
2. In the present disclosure, the low-temperature condensate can be freely distributed to
the plurality of shift stripping towers according to the operation state of the condensate
stripping towers. Moreover, the ammonia recovery device purifies the shift condensate by means of optimal combination of the low-temperature condensate and the sulfur-containing
low-concentration ammonia water to produce the high-purity gas ammonia and ammonia water with different concentrations, which solves the problems of water equilibrium and
ammonia equilibrium in the boiler desulfurization system and greatly improves the quality of
ammonium sulfate. Part of the gas ammonia produced is used for boiler denitration, which
reduces the cost for purchasing liquid ammonia for the boiler. Further, the excess ammonia is
used for preparing ammonia water to be sold, which greatly reduces the production cost and meets the requirement of the stable operation of the system. Upon testing, the benefit
generated is 18.9203 million yuan per year. 3. In the present disclosure, the shift condensate treatment process cooperates with the
ammonia recovery process, thereby meeting the requirement for the treatment of the shift
condensate in the three systems. That is, the shift stripping towers can be operated flexibly to
adjust their treatment amounts or to stop operation. Moreover, after the shift condensate is
purified, the waste is converted into valuable substances. A variety of ammonia products can be produced to meet a variety of demands, thereby realizing the urgency and practicability of
industrial production.
The accompanying drawings constituting a part of the present disclosure are used for
providing further understanding for the present disclosure. Exemplary embodiments of the
present disclosure and descriptions thereof are used for explaining the present disclosure and
do not constitute any inappropriate limitation to the present disclosure.
FIG. 1 is a schematic diagram of a shift condensate treatment process according to an
embodiment the present disclosure; and FIG. 2 is a schematic diagram of an ammonia recovery process according to an embodiment the present disclosure.
In the figures: fl, first valve; f2, second valve; f3, third valve; f4, first outgoing valve; f5,
second outgoing valve; f6, third outgoing valve; f7, first ammonia recovery valve; f8, second
ammonia recovery valve; f9, first desulfurization valve; fl, second desulfurization valve; 1,
shift I stripping tower; 2, shift II stripping tower; 3, shift III stripping tower; 4, ammonia
water tower; 5, raw water tank; 6, stripping tower; 7, three-stage partial condenser; 8, refining
tower; 9, ammonia water preparation device. In order to show positions of parts, the distance between parts or the size of each part is
exaggerated, and the schematic diagrams are for illustrative use only.
For the convenience of description, the terms "up", "down", "left" and "right" in the
present disclosure only indicate that they are consistent with the up, down, left and right
directions of the drawing itself, and do not constitute a limitation to the structure. They are
merely for ease of describing the present disclosure and simplifying the description, and do not indicate or imply that the apparatus or element referred to must have a specific orientation,
or be constructed and operated in a specific orientation, so they cannot be understood as
limiting the present disclosure. In the present disclosure, the terms "mounting", "linking", "connection", "fixing" and the like should be understood in a broad sense. For example, the
connection may be a fixing connection, a detachable connection or an integral connection; or
may be a mechanical connection; or may be a direct connection, or an indirect connection by
using an intermediary; or may be an internal connection between two elements or an interaction between two elements. Those of ordinary skill in the art may determine the
specific meanings of the foregoing terms in the present disclosure according to specific
situations. In the field of chemical industry, a shift low-temperature condensate and
sulfur-containing low-concentration ammonia water are collectively referred to as a shift
condensate.
As described in the background, low-concentration ammonia water contains H2S, C02,
CO, H2, iron ions, etc., which affects the efficiency of flue gas desulfurization and the quality of the byproduct ammonium sulfate, and destroys the ammonia equilibrium and water equilibrium, causing excess and escape of ammonia. Moreover, when the shift stripping towers treat the low-temperature condensate, it is impossible to stop operation of a single shift stripping tower for maintenance, which affects the long-term stable operation of the system. In order to solve the above technical problems, the present disclosure provides a shift condensate treatment system. As shown in FIG. 1 to FIG. 2, an embodiment of the present disclosure provides a shift condensate treatment system, including: at least two shift stripping towers and an ammonia recovery device. Inlets of two of the shift stripping towers are respectively connected to shift low-temperature condensate pipelines, and outlets are connected to a sulfur-containing low-concentration ammonia water pipeline. The two shift low-temperature condensate pipelines are respectively provided with a first pipeline connected to an inlet of the ammonia recovery device. The sulfur-containing low-concentration ammonia water pipeline is provided with a second pipeline connected to the inlet of the ammonia recovery device. An outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline. The sulfur-containing low-concentration ammonia water pipeline is configured to be connected to a boiler ammonia desulfurization apparatus.
The stripping process based on shift stripping towers is used to treat the shift condensate.
The number of the low-temperature condensate pipelines is greater than that of the corresponding shift stripping tower pipelines, the corresponding ammonia recovery process
pipeline is added, and the plurality of shift low-temperature condensate pipelines converge to
the stripping tower of the ammonia recovery process, thereby reducing the treatment amount
of the shift stripping tower. When one of the shift stripping towers breaks down, the
low-temperature condensate may be treated by the ammonia recovery device or the other
shift stripping towers, which solves the problem that it is impossible to stop operation of a
single shift stripping tower and improves the flexibility in the operation of three parallel shift condensate systems. Thereby, there are many operation modes to be selected, which reduces
unnecessary start-up and shutdown costs and avoids fluctuations of the system caused by start-up and shutdown for shift and heat recovery. The sulfur-containing low-concentration
ammonia water subjected to shift stripping and the low-temperature condensate are mixed to the ammonia recovery device for treatment. After the treatment, the high-purity ammonia is extracted and used for boiler ammonia desulfurization, which ensures the continuous and stable operation of the shift system and the boiler desulfurization system.
On the basis of the original process, the plurality of shift low-temperature condensate
pipelines are communicated with the inlet of the stripping process, a valve is added to each pipeline, and all the pipelines converge and are connected to the new treatment process
(ammonia recovery device). After the low-temperature condensate is treated, the sulfur-containing low-concentration ammonia water is obtained. On the basis of the original
process, the sulfur-containing low-concentration ammonia water pipeline is connected to the
new treatment process (ammonia recovery device), and a valve is added to this pipeline. In
this way, the treatment modes can be switched at any time.
The number of shift low-temperature condensate processes is 1.5 times that of the stripping treatment processes. In this embodiment, there are 2 stripping treatment processes
(one includes shift I, shift II and shift III stripping towers, and the other includes the stripping tower in the ammonia recovery), corresponding to 3 shift low-temperature condensate
processes (i.e., ShiftI, Shift II and Shift III in FIG. 1); or the load of each shift stripping
tower treating the low-temperature condensate is reduced to 60%, or the operation of a single
shift stripping tower system is stopped.
As shown in FIG. 1, in an example of three sets of shift condensate, the three sets of shift low-temperature condensate correspond to three shift stripping towers, and a first valve fl, a
second valve f2 and a third valve 3 are fully opened. By adding the treatment pipeline, the
three sets of shift low-temperature condensate can enter the ammonia recovery device.
Alternatively, openings of the first valve fl, the second valve f2, the third valve 3 and a first
ammonia recovery valve f7 may be adjusted to control the three shift stripping towers to
operate under different loads or to stop operation.
In the prior art, the sulfur-containing low-concentration ammonia water obtained after treating the low-temperature condensate by the shift stripping tower corresponds to boiler
ammonia desulfurization, and a first desulfurization valve 9 is fully opened. By adding the
treatment pipeline and a second ammonia recovery valve 8, the sulfur-containing
low-concentration ammonia water may enter the ammonia recovery device for treatment. The refined ammonia water is used for boiler ammonia desulfurization through the added pipeline and a second desulfurization valve flO. Alternatively, the second ammonia recovery valve f8 and the first desulfurization valve f may be adjusted to control the ammonia recovery device to operate under different loads.
Further, improvements to the three shift condensate pipelines include: on the three shift system low-temperature condensate pipelines, an outgoing condensate pipeline is connected
respectively before the first valve fl, the second valve f2 and the third valve 3, and the three pipelines are connected to an outgoing shift condensate main pipe; and before the first
desulfurization valve f9, a pipeline to ammonia recovery is connected on the
sulfur-containing low-concentration ammonia water pipeline, and the shift condensate
subjected to the ammonia recovery is refined to obtain concentrated ammonia water, which is
connected to the pipeline after the first desulfurization valve
. As shown in FIG. 2, the ammonia recovery device includes a stripping tower 6
configured to treat the shift condensate. The stripping tower 6 has a shift condensate inlet in a middle, and the shift condensate inlet corresponds to the plurality of shift condensate
pipelines. A liquid-phase inlet of the stripping tower 6 further includes a raw water tank 5
used for optimal combination of the shift condensates. The stripping tower 6 has an acid gas
blow-down pipeline at a top, and a purified water discharge pipeline at a bottom. A pipeline is
led out from the middle of the stripping tower 6, and the middle of the stripping tower 6 is connected to a partial condenser 7 so as to deliver rich ammonia gas in the partial condenser
7. An upper part of the three-stage partial condenser 7 is connected to the refining tower 8 so
as to deliver crude ammonia gas into the refining tower 8. The partial condenser 7 and the
refining tower 8 are both used to further remove acid gases such as H2S and C02. A pipeline
is led out from a top of the refining tower 8 and respectively connected to a boiler denitration
device and an ammonia water preparation device 9. The ammonia water preparation device 9
is configured to prepare ammonia water with different concentrations, which is connected to a boiler desulfurization device or is sold.
It should be understood that the shift condensate ( low-temperature condensate and
sulfur-containing low-concentration ammonia water) subjected to optimal combination enters
the stripping tower 6 from the middle; according to the characteristic that relative volatilities of hydrogen sulfide and the carbon dioxide are higher than the relative volatility of ammonia, the hydrogen sulfide and the carbon dioxide of the shift condensate are first stripped from the top of the stripping tower 6; the temperature in the stripping tower 6 forms a temperature gradient from top to bottom by the steam at the bottom, the shift condensate entering the tower that has subjected to heat exchange to different temperatures, and the cold feed at the top of the stripping tower 6; the temperature of the middle of the stripping tower is controlled to 150-155°C such that the ammonia can be drawn out from the side line; a variable-temperature variable-pressure method based on the three-stage partial condenser 7 is used to obtain relatively pure ammonia gas, which is passes through the refining tower 8 to further remove the acid gases such as H2S and CO 2 so as to prepare high-purity ammonia gas; and the high-purity ammonia gas is sent to the user, or used to prepare ammonia water with different concentrations, which is then sent to the user. After the improvement, since each set of shift condensate corresponds to different treatment processes, the treatment loads of the shift I stripping tower 1, the shift II stripping tower 2 and the shift III stripping tower 3 are reduced, and the operation condition and running are also optimized, thereby reducing the consumption of steam. The rest is treated by the ammonia recovery device. The operating loads of the three shift stripping towers and the operating load of the ammonia recovery device can be adjusted flexibly according to the operation needs. On the one hand, the treatment amounts of the shift stripping towers can be reduced, thereby reducing the corrosion of the system. On the other hand, after the shift condensate is treated by the ammonia recovery device, the acid gases can be separated from the ammonia, so that the ammonia products are purer, and high-purity gas ammonia and ammonia water with different concentrations can be produced, which solves the problems of water equilibrium and ammonia equilibrium in the boiler desulfurization system and greatly improves the quality of ammonium sulfate. Part of the gas ammonia produced is used for boiler denitration, thereby well meeting the use in boiler desulfurization and denitration. Due to the presence of carbon dioxide, ammonia and water vapor, if the enriched ammonia gas at the middle of the stripping tower 6 is cooled at one time to obtain ammonia gas, ammonium salt crystals will be generated, which not only affects the ammonia recovery rate, but also blocks the apparatus and pipelines. Therefore, a method of reducing the temperature and pressure stage by stage, that is, a three-stage partial condenser 7, is used to separate the ammonia from carbon dioxide.
A bottom of the three-stage partial condenser 7 is connected to the raw water tank 5 for
retreatment.
Due to the presence of part of acid gases in the crude ammonia gas on the upper part of
the three-stage partial condenser 7, it is required to perform further desulfurization and
decarbonization. The refining tower 8 is divided into an upper section and a lower section. At the lower section, more than 95% of carbon dioxide and hydrogen sulfide are removed, and a
solution is used cyclically for absorption. At the upper section, fresh low-temperature
concentrated ammonia water is used to deeply remove the remaining carbon dioxide and
hydrogen sulfide.
Preferably, an upper part of the refining tower 8 is provided with a gas-phase outlet,
which is configured to be connected to the user.
The refining tower 8 is connected to the ammonia water preparation device 9, which is configured to prepare ammonia water with different concentrations. The ammonia water can
be used for boiler ammonia desulfurization or be sold, which depends on the process
requirements or the user demands. The pipeline led out from the middle of the stripping tower
is connected to the partial condenser, the partial condenser is connected to the refining tower,
and desulfurization and decarbonization are performed in the refining tower to produce the
high-purity gas ammonia. One part of the gas ammonia is used for SCR denitration of flue
gas, and the other part is sent to the ammonia water preparation device. One part of the cyclically prepared concentrated ammonia water is used for ammonia desulfurization, and the
other part is sent to an ammonia water storage tank, so that ammonia water with different
concentrations can be up for sale.
This embodiment provides a shift condensate treatment process, including: converting a
shift low-temperature condensate into sulfur-containing low-concentration ammonia water by
a shift stripping tower, the sulfur-containing low-concentration ammonia water being used for
ammonia desulfurization, and a number of the shift stripping towers being at least two; enabling, according an operating state, part or all of the shift low-temperature condensate to
enter an ammonia recovery device for purification without passing through the shift stripping towers and then be used for the ammonia desulfurization; and enabling, according to the operating state, part or all of the sulfur-containing low-concentration ammonia water to enter the ammonia recovery device for purification and then be used for the ammonia desulfurization. Upon testing, the pure ammonia output of the ammonia recovery device is 823 kg/h, so
6584 tons of liquid ammonia less is purchased per year. In addition, 48 tons of liquid
ammonia is needed as a supplement to the index fluctuation of boiler operation exhaust, so 6536 tons of liquid ammonia needs to be purchased per year. According to the same
calculation criterion that the price of liquid ammonia is 3465 yuan/ton, the cost of purchasing
liquid ammonia will be reduced by 22.6472 million yuan per year, and the operating cost of
4.5189 million yuan is deducted therefrom, so it is estimated that the benefit will be 18.1283
million yuan per year. After the quality of the ammonium sulfate product is improved, the
unit price is increased by 40 yuan/ton, and according to the average output of 60 tons per day,
the benefit of the product is increased by 0.792 million yuan per year. The total benefit is 18.9203 million yuan per year.
In the prior art, the shift low-temperature condensate can be treated only by the
respective shift stripping towers, and the sulfur-containing low-concentration ammonia water
is used for boiler ammonia desulfurization. Limited by the flow and process, the condensate
stripping tower is high in operating load and prone to corrosion, and the produced
sulfur-containing low-concentration ammonia water has high contents of impurities such as
acid gases and metal ions, which severely affects the water equilibrium and desulfurization effect of the desulfurization system and makes the system difficult to realize ammonia
equilibrium, causing escape of ammonia (secondary pollution) and waste of resources and
poor quality of byproducts such as ammonium sulfate, and thus affecting the stable operation
of the boiler desulfurization system. In the present disclosure, the low-temperature
condensate can be freely distributed to the three shift stripping towers according to the
operation state of the condensate stripping towers, which reduces the treatment amounts of
the shift condensate stripping towers and solves the problem that it is impossible to stop operation of a single shift stripping tower, thereby realizing flexible operation of the shift
condensate systems and reducing the start-up and shutdown costs of 100000 RMB/time.
Moreover, the ammonia recovery device purifies the shift condensate by means of optimal
combination of the low-temperature condensate and the sulfur-containing low-concentration ammonia water to produce the high-purity gas ammonia and ammonia water with different
concentrations, which solves the problems of water equilibrium and ammonia equilibrium in
the boiler desulfurization system and greatly improves the quality of ammonium sulfate. Part of the gas ammonia produced is used for boiler denitration, which reduces the cost for
purchasing liquid ammonia for the boiler. Further, the excess ammonia is used for preparing ammonia water to be sold, which greatly reduces the production cost and meets the
requirement of the stable operation of the system.
No matter how to improve the shift condensate treatment pipelines and process, the same
effect can be achieved as long as the three sets of shift condensate can correspond to different
treatment methods to realize flexible operation. Although the specific implementations of the present disclosure are described above with
reference to the accompanying drawings, they are not intended to limit the protection scope of the present disclosure. It should be appreciated by a person skilled in the art that: various
modifications or variations that can be made to the technical solutions of the present
disclosure without creative work shall fall within the protection scope of the present
disclosure.
Claims (7)
1. A shift condensate treatment system, comprising at least two shift stripping towers and an ammonia recovery device; wherein
inlets of the shift stripping towers are connected to shift low-temperature condensate
pipelines, and outlets are connected to a sulfur-containing low-concentration ammonia water
pipeline; the shift low-temperature condensate pipelines are respectively provided with a first
pipeline connected to an inlet of the ammonia recovery device; the sulfur-containing
low-concentration ammonia water pipeline is provided with a second pipeline connected to
the inlet of the ammonia recovery device; an outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third
pipeline; the sulfur-containing low-concentration ammonia water pipeline is configured to be
connected to a boiler ammonia desulfurization apparatus;
the sulfur-containing low-concentration ammonia water pipeline is provided with an
ammonia water tower; the ammonia recovery device comprises a stripping tower; the
stripping tower has a shift condensate inlet in a middle, and the shift condensate inlet
corresponds to the plurality of shift low-temperature condensate pipelines; the stripping tower has an acid gas blow-down pipeline at a top, and a purified water discharge pipeline at a
bottom; the ammonia recovery device further comprises a three-stage partial condenser, a
pipeline led out from the middle of the stripping tower being connected to the three-stage
partial condenser; and the ammonia recovery device further comprises a refining tower, an
upper part of the three-stage partial condenser being connected to the refining tower.
2. The shift condensate treatment system according to claim 1, wherein a number of the
shift stripping towers is three, and the outlets of the three shift stripping towers are all
connected to the ammonia water tower.
3. The shift condensate treatment system according to claim 1, wherein the ammonia
recovery device further comprises a raw water tank, and a bottom of the three-stage partial
condenser is connected to the raw water tank.
4. The shift condensate treatment system according to claim 1, wherein the refining tower is divided into an upper section and a lower section; at the lower section, at least 95% of carbon dioxide and hydrogen sulfide are removed, and a solution is used cyclically for absorption; and at the upper section, fresh low-temperature concentrated ammonia water is used to deeply remove the remaining carbon dioxide and hydrogen sulfide.
5. The shift condensate treatment system according to claim 4, wherein the ammonia recovery device further comprises an ammonia water preparation device, a pipeline led out of
a top of the refining tower being connected to the ammonia water preparation device, and the ammonia water preparation device being configured to prepare ammonia water with different
concentrations.
6. A shift condensate treatment process using the shift condensate treatment system
according to any of claims 1 to 5, comprising:
converting a shift low-temperature condensate into sulfur-containing low-concentration ammonia water by a shift stripping tower, a number of the shift stripping towers being at least
two; enabling, according an operating state, part or all of the shift low-temperature
condensate to enter an ammonia recovery device for purification without passing through the
shift stripping towers and then be used for ammonia desulfurization; and
enabling, according to the operating state, part or all of the sulfur-containing
low-concentration ammonia water to enter the ammonia recovery device for purification and then be used for the ammonia desulfurization;
wherein the purification in the ammonia recovery device comprises: after the shift
low-temperature condensate enters a stripping tower, ammonia-rich gas in which part of acid
gas has been removed is drawn out from a middle of the stripping tower and then sent to a
three-stage partial condenser; in the three-stage partial condenser, the acid gas is further
removed, and crude ammonia gas is obtained from a top, which is sent to a refining tower;
and in the refining tower, the acid gas is deeply removed.
7. The shift condensate treatment process according to claim 6, wherein the refined
ammonia gas in the refining tower is sent into an ammonia water preparation device, and
ammonia water prepared by the ammonia water preparation device is used for boiler
ammonia desulfurization or is sold.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210842707.1 | 2022-07-18 | ||
| CN202210842707.1A CN115259259B (en) | 2022-07-18 | 2022-07-18 | System and process for treating conversion condensate |
| PCT/CN2023/107744 WO2024017202A1 (en) | 2022-07-18 | 2023-07-17 | Shift condensate treatment system and process |
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| AU2023296338A1 true AU2023296338A1 (en) | 2024-02-08 |
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| AU2023296338A Pending AU2023296338A1 (en) | 2022-07-18 | 2023-07-17 | Shift condensate treatment system and process |
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| CN (1) | CN115259259B (en) |
| AU (1) | AU2023296338A1 (en) |
| WO (1) | WO2024017202A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4573106B2 (en) * | 2004-12-20 | 2010-11-04 | 昌弘 小川 | A method for separating and recovering ammonia and hydrogen sulfide from desulfurization wastewater. |
| US9901861B2 (en) * | 2011-10-18 | 2018-02-27 | General Electric Technology Gmbh | Chilled ammonia based CO2 capture system with wash system and processes of use |
| WO2015102136A1 (en) * | 2014-01-06 | 2015-07-09 | (주)에이엠티퍼시픽 | Energy saving type method for removing acid gas through pretreatment using ammonia water |
| CN206325247U (en) * | 2016-11-15 | 2017-07-14 | 中化重庆涪陵化工有限公司 | Energy saving technique condensate liquid stripping system |
| CN106582272B (en) * | 2016-12-14 | 2019-11-15 | 山东迅达化工集团有限公司 | The desulfurizing and purifying technique of sour water stripping ammonia |
| CN208732630U (en) * | 2018-08-28 | 2019-04-12 | 陕西长青能源化工有限公司 | A kind of transformation condensate liquid pre-concentration double tower stripping ammonia recovery unit |
| CN209872642U (en) * | 2019-04-09 | 2019-12-31 | 中化重庆涪陵化工有限公司 | Synthetic ammonia low transformation gas technology condensate purification treatment system |
| CN110203986B (en) * | 2019-05-16 | 2022-01-14 | 中国神华煤制油化工有限公司 | System and method for reducing ammonia nitrogen content |
| CN113528196B (en) * | 2021-08-06 | 2022-04-12 | 陕西未来能源化工有限公司 | Shifted gas treatment or improvement process and low-temperature methanol washing device and process |
| CN115259259B (en) * | 2022-07-18 | 2023-06-16 | 陕西未来能源化工有限公司 | System and process for treating conversion condensate |
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| WO2024017202A1 (en) | 2024-01-25 |
| CN115259259A (en) | 2022-11-01 |
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