CN115259259A - Conversion condensate treatment system and process - Google Patents
Conversion condensate treatment system and process Download PDFInfo
- Publication number
- CN115259259A CN115259259A CN202210842707.1A CN202210842707A CN115259259A CN 115259259 A CN115259259 A CN 115259259A CN 202210842707 A CN202210842707 A CN 202210842707A CN 115259259 A CN115259259 A CN 115259259A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- shift
- condensate
- ammonia water
- low
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
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 invention relates to the technical field of coal chemical industry, in particular to a system and a process for treating conversion condensate. The shift condensate treatment system includes: at least two shift stripper columns and an ammonia recovery unit; the inlets of the two shift stripping towers are respectively connected with a shift low-temperature condensate pipeline, the outlet of the two shift stripping towers is a sulfur-containing low-concentration ammonia water pipeline, the two shift low-temperature condensate pipelines are respectively provided with a first pipeline connected to the 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, the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline, and the sulfur-containing low-concentration ammonia water pipeline is used for being connected to boiler ammonia desulphurization equipment; the problem that the single tower can not exit when the conversion stripping tower is maintained is solved, and the stable operation of the system is ensured.
Description
Technical Field
The invention relates to the technical field of coal chemical industry, in particular to a system and a process for treating conversion condensate.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
The conversion condensate is low-temperature condensate and sulfur-containing low-concentration ammonia water, the low-temperature condensate is water gas-215 ℃ from gasification, the condensate separated when the conversion gas is reduced to below 90 ℃ is gradually cooled after partial conversion reaction, and the condensate contains ammonia, hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, iron ions and the like; the low-concentration ammonia water containing sulfur means lowSteam stripping the warm condensate in a shift stripping tower, gasifying the liquid phase, condensing and desalting the gas phase to produce low concentration ammonia water containing sulfur and H dissolved in the ammonia water2S、CO2、CO、H2And iron ions, and the like.
Low-temperature condensate generated by condensing water gas of the conversion system is stripped through a stripping tower, low-concentration ammonia water is sent to an ammonia-process desulfurization system of boiler flue gas after gas phase is subjected to condensation and desalted water washing treatment, and the low-concentration ammonia water contains H2S、CO2、CO、H2Iron ions and the like, which affect the efficiency of flue gas desulfurization and the quality of ammonium sulfate as a byproduct, and destroy the ammonia balance and water balance, thereby causing excessive ammonia and escape; and meanwhile, when the low-temperature condensate is treated by the conversion stripping tower, the working condition of equipment is poor, the corrosion leakage phenomenon often occurs, and the single tower can not be withdrawn during maintenance, so that the long-period stable operation of the system is influenced.
Disclosure of Invention
Aiming at the defects in the prior art, the embodiment of the invention aims to provide a conversion condensate treatment system, which solves the problems of water balance and ammonia balance of a boiler desulfurization system and improves the quality of ammonium sulfate; the problem that the shift stripping tower cannot exit from a single tower during maintenance is solved, and the stable operation of the system is ensured.
In order to achieve the above object, the embodiments of the present invention provide the following technical solutions:
a shift condensate treatment system comprising: at least two shift stripper columns and an ammonia recovery unit; the inlets of the two conversion stripping towers are respectively connected with a conversion low-temperature condensate pipeline, the outlet of the two conversion low-temperature condensate pipelines is a sulfur-containing low-concentration ammonia water pipeline, the two conversion low-temperature condensate pipelines are respectively provided with a first pipeline connected to the 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, the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline, and the sulfur-containing low-concentration ammonia water pipeline is used for being connected to boiler ammonia-method desulfurization equipment.
In another preferred embodiment, an ammonia water tower is arranged on the sulfur-containing low-concentration ammonia water pipeline, the 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 embodiment, the ammonia recovery unit comprises a stripping column having a shift condensate inlet in the middle thereof, the shift condensate inlet corresponding to multiple shift condensate lines, the stripping column having an acid gas vent line at the top thereof and a purified water discharge line at the bottom thereof.
In another preferred embodiment, the ammonia recovery device further comprises a three-stage partial condenser, and the middle outlet pipeline of the stripping tower is connected with the three-stage partial condenser.
In another preferred embodiment, the ammonia recovery device further comprises a raw water tank, and the bottom of the three-stage partial condenser is connected with the raw water tank.
In another preferred embodiment, the ammonia recovery device further comprises a refining tower, the upper part of the three-stage partial condenser is connected with the refining tower, the refining tower is divided into two sections, at least 95% of carbon dioxide and hydrogen sulfide are removed in the lower section, and the solution is circularly absorbed; and the upper section uses fresh low-temperature concentrated ammonia water to deeply remove the residual carbon dioxide and hydrogen sulfide.
In another preferred embodiment, the ammonia recovery device further comprises an ammonia water preparation device, the pipeline led out from the top of the refining tower is connected with the ammonia water preparation device, and the ammonia water preparation device is used for preparing different strong ammonia water.
The embodiment of the invention also provides a method for processing the conversion condensate, which comprises the following steps: the shift low-temperature condensate is converted into sulfur-containing low-concentration ammonia water through a shift stripping tower, the sulfur-containing low-concentration ammonia water is used for ammonia desulphurization, and the number of the shift stripping towers is at least two; according to the operation condition, selecting part or all of low-temperature condensate to enter an ammonia recovery device without a transformation stripping tower for purification and then using the condensate for ammonia desulphurization; according to the operation condition, part or all of the sulfur-containing low-concentration ammonia water is selected to enter an ammonia recovery device for purification and then is used for ammonia desulphurization.
In another preferred embodiment, the ammonia recovery device purification comprises: the conversion condensate enters a stripping tower, rich ammonia gas with part of acid gas removed is extracted from the middle part of the stripping tower and enters a three-stage partial condenser, crude ammonia gas is obtained at the top after further separation with the acid gas in the three-stage partial condenser and enters a refining tower, and the acid gas is deeply removed in the refining tower.
In another preferred embodiment, the ammonia gas refined in the refining tower is sent to an ammonia water preparation device, and the ammonia water prepared by the ammonia water preparation device is sent to a boiler for ammonia desulphurization or ammonia water sale.
One or more technical solutions provided in the embodiments of the present invention have at least the following technical effects or advantages:
1. the invention adopts the steam stripping process of the conversion stripping tower to treat the conversion condensate, the low-temperature condensate pipelines are more than the corresponding conversion stripping tower pipelines, the corresponding ammonia recovery process pipelines are added, a plurality of conversion low-temperature condensate pipelines are mixed to the ammonia recovery process stripping tower for treatment, the treatment capacity of the conversion stripping tower is reduced, when one conversion stripping tower is in trouble and stops working, the low-temperature condensate can be treated by an ammonia recovery device or other conversion stripping towers, the problem that a single conversion stripping tower cannot exit is solved, the running of three parallel conversion condensate systems has greater flexibility, the running modes have various choices, the unnecessary running and stopping expenses are reduced, and the fluctuation of the systems caused by conversion and heat recovery starting and stopping is avoided. The sulfur-containing low-concentration ammonia water subjected to conversion stripping treatment and the low-temperature condensate are mixed to an ammonia recovery device for treatment, and high-purity ammonia is extracted after treatment and is sent to a boiler for ammonia desulphurization, so that the problems of water balance and ammonia balance of a boiler desulphurization system are solved, the quality of ammonium sulfate is improved, and the continuous and stable operation of a conversion and heat recovery system and the boiler desulphurization system is ensured.
2. According to the invention, free distribution of multiple sets of conversion to low-temperature condensate according to the operation condition of the condensate stripping tower is realized, and meanwhile, the ammonia recovery device realizes purification treatment of the conversion condensate through optimized combination of the low-temperature condensate and the sulfur-containing dilute ammonia water, so that high-purity gas ammonia and ammonia water with different concentrations are produced, the problems of water balance and ammonia balance of a boiler desulfurization system are solved, the quality of ammonium sulfate is greatly improved, part of produced gas ammonia is used for boiler denitration, the cost of purchasing liquid ammonia from a boiler is reduced, meanwhile, the surplus ammonia is made into ammonia water for sale, the production cost is greatly reduced, and stable operation of the system is satisfied. The test shows that the benefit is 1892.03 ten thousand yuan/year.
3. The conversion condensate treatment process and the ammonia recovery process are matched with each other, the conversion condensate treatment requirements in three systems are met, namely the conversion stripping tower treatment capacity is flexibly operated and quit, the conversion condensate is purified and treated to change waste into valuable, and the ammonia product diversification and multiple requirements meet the urgency and practicability of industrial production.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic view of a shift condensate treatment process according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of an ammonia recovery process according to an embodiment of the present invention;
in the figure: f1, a first valve; f2, a second valve; f3, a third valve; f4, a first delivery valve; f5, a second outward delivery valve; f6, a third delivery valve; f7, a first ammonia recovery valve; f8, a second ammonia recovery valve; f9, a first desulfurization valve; f10, a second desulfurization valve; 1. Changing into a stripping tower; 2. changing into a second stripping tower; 3. a triple stripping tower; 4. an ammonia tower; 5. a raw material water tank; 6. a stripping column; 7. a third-stage dephlegmator; 8. a refining tower; 9. preparing an ammonia water device;
the spacing or dimensions between each other are exaggerated to show the location of the various parts, and the illustration is for illustrative purposes only.
Detailed Description
For convenience of description, the words "up", "down", "left" and "right" in the present application, if any, merely indicate correspondence with the directions of up, down, left and right of the drawings themselves, and do not limit the structure, but merely facilitate the description of the invention and simplify the description, rather than indicate or imply that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, are not to be construed as limiting the invention. The terms "mounted," "connected," "fixed," and the like in the present invention are to be understood broadly, and for example, they may be fixedly connected, detachably connected, or integrated; the term "coupled" may refer to a mechanical coupling, a direct coupling, an indirect coupling via an intermediate, an internal coupling of two elements, or an interaction of two elements, and it is understood that the terms used in the present invention have the same meaning as the terms used in the present invention. In the chemical field, the transformation low-temperature condensate and the sulfur-containing low-concentration ammonia water are collectively called transformation condensate.
As described in the background, low concentration aqueous ammonia contains H2S、CO2、CO、H2Iron ions and the like, which affect the efficiency of flue gas desulfurization and the quality of ammonium sulfate as a byproduct, and destroy the ammonia balance and water balance to cause excessive and escaping of ammonia; meanwhile, when the low-temperature condensate is treated by the shift stripping tower, the single tower can not be withdrawn for maintenance, and the long-period stable operation of the system is influenced. In order to solve the technical problem, the invention provides a conversion condensate treatment system.
As shown in fig. 1-2, in one embodiment of the present invention, a shift condensate treatment system is described, comprising: at least two shift stripper columns and an ammonia recovery unit; the inlets of the two conversion stripping towers are respectively connected with a conversion low-temperature condensate pipeline, the outlet of the two conversion low-temperature condensate pipelines is a sulfur-containing low-concentration ammonia water pipeline, the two conversion low-temperature condensate pipelines are respectively provided with a first pipeline connected to the 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, the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentration ammonia water pipeline through a third pipeline, and the sulfur-containing low-concentration ammonia water pipeline is used for being connected to boiler ammonia-method desulfurization equipment.
Adopt the conversion stripping tower steam stripping technology to handle the conversion condensate, low temperature condensate pipeline is more than the conversion stripping tower pipeline that corresponds, increase and correspond ammonia recovery process pipeline, many conversion low temperature condensate pipelines mix and handle to ammonia recovery process stripping tower, the handling capacity of conversion stripping tower has been reduced, when one set of conversion stripping tower goes wrong and stops work, low temperature condensate can be handled through ammonia recovery unit or other conversion stripping towers, the problem that single set of conversion stripping tower can't withdraw from has been solved, make the operation of parallel three sets of conversion condensate systems have had bigger flexibility, multiple choice has been gone up on the operation mode, reduce unnecessary and open, the parking expense, the fluctuation of starting the parking and causing the system because of conversion and heat recovery has been avoided. The sulfur-containing low-concentration ammonia water subjected to conversion stripping treatment and the low-temperature condensate are mixed to an ammonia recovery device for treatment, high-purity ammonia is extracted after treatment and sent to a boiler for ammonia desulphurization, and continuous and stable operation of a conversion system and a boiler desulphurization system is maintained.
On the basis of the original process, a plurality of low-temperature condensate conversion pipelines are communicated with a steam stripping process inlet, a valve is added on each pipeline, and simultaneously, each pipeline is mixed and connected with a newly-added treatment process (an ammonia recovery device); the low-concentration ammonia water containing sulfur is obtained after the low-temperature condensate is treated, on the basis of the original process, the pipeline of the low-concentration ammonia water containing sulfur is connected with a newly added treatment process (an ammonia recovery device), a valve is added on the pipeline, and the treatment mode is switched at any time.
The number of the processes for transforming the low-temperature condensate is 1.5 times of that of the stripping treatment process. In the embodiment, the steam stripping treatment process is 2 sets (one set of stripping tower is changed into one set of stripping tower, two sets of stripping tower and three sets of stripping tower are changed into one set of stripping tower in ammonia recovery), and corresponds to 3 sets of low-temperature condensate conversion processes (namely conversion I, conversion II and conversion III in figure 1); or, each set of conversion stripping tower is used for treating low-temperature condensate to reduce the load to 60 percent, or a single set of conversion stripping tower system is withdrawn.
As shown in fig. 1, taking three sets of conversion condensate as an example, three sets of conversion low-temperature condensate are processed and operated corresponding to three sets of conversion stripping towers, a first valve f1, a second valve f2 and a third valve f3 are operated in a fully-opened manner, the three sets of conversion low-temperature condensate can enter an ammonia recovery device by adding the three sets of conversion low-temperature condensate in a processing pipeline, and the three sets of conversion stripping towers can be adjusted to operate or quit operating under different loads by adjusting the opening degrees of the first valve f1, the second valve f2, the third valve f3 and a first ammonia recovery valve f 7;
in the prior art, the sulfur-containing low-concentration ammonia water treated by the low-temperature condensate in the shift stripping tower operates corresponding to the ammonia valve of the boiler for desulfurization, and the first desulfurization valve f9 operates in a fully-opened mode. The refined ammonia water enters the boiler for ammonia desulphurization operation through the added pipeline and the second desulphurization valve f 10; the ammonia recovery device can be adjusted to operate under different loads through the second ammonia recovery valve f8 and the first desulfurization valve f 9.
Further, the three sets of process pipelines for improving the conversion condensate pipelines mean that three sets of low-temperature condensation pipelines of the conversion system are respectively connected with an outward-feeding condensate pipeline in front of a first valve f1, a second valve f2 and a third valve f3, and three pipelines are connected to an outward-feeding conversion condensate main pipe; the front pipeline of the first desulfurization valve f9 is connected with an ammonia recovery processing pipeline, and the converted condensate after ammonia recovery processing is refined into concentrated ammonia water which is connected with the rear pipeline of the first desulfurization valve f 9.
As shown in fig. 2, the ammonia recovery device comprises a stripping tower 6 for treating shift condensate, wherein a shift condensate inlet is arranged in the middle of the stripping tower 6 and corresponds to a plurality of shift condensate pipelines; the liquid phase inlet of the stripping tower 6 also comprises a raw material water tank 5 which is used for optimizing and combining the conversion condensate; an acid gas emptying pipeline is arranged at the top of the stripping tower 6; the bottom is provided with a purified water discharge pipeline. A pipeline is led out from the middle part of the stripping tower 6, and a partial condenser 7 is connected to the middle part of the stripping tower 6 and is used for conveying rich ammonia gas into the partial condenser 7. The upper part of the three-stage partial condenser 7 is connected with a refining tower 8 and is used for conveying crude ammonia gas into the refining tower 8. The partial condenser 7 and the refining tower 8 are used for further removing H2S、CO2And the like acid gases. A pipeline is led out from the top of the refining tower 8 and is respectively connected with a boiler pin removal device and an ammonia water preparation device 9; the ammonia water preparing device 9 is used for preparing different strong ammonia water and is connected with a boiler desulphurization device or the ammonia water for sale.
It should be understood that the shift conversion condensate (low-temperature condensate and sulfur-containing low-concentration ammonia water) enters the stripping tower 6 from the middle part of the stripping tower after being optimally combined, the hydrogen sulfide and the carbon dioxide of the shift conversion condensate are stripped from the top of the stripping tower 6 according to the characteristic that the relative volatility of the hydrogen sulfide and the carbon dioxide is higher than that of ammonia, and the temperature of the stripping tower 6 passes through bottom steam and enters the stripping towerChanging different temperatures of the condensate after heat exchange and cold feed at the top of the tower to form a temperature gradient from top to bottom in a stripping tower 6, controlling the temperature at 150-155 ℃ in the middle of the stripping tower to carry out side draw of ammonia, obtaining purer ammonia gas by using a three-stage partial condenser 7 with variable temperature and variable pressure, and further removing H through a refining tower 82S、CO2And (3) waiting for the acid gas to prepare high-purity ammonia gas, and sending the high-purity ammonia gas to a user or preparing ammonia water with different concentrations, and then sending the ammonia water to the user.
Because each set of the improved conversion condensate corresponds to different treatment processes, the treatment loads in the improved one-to-one stripping tower 1, the improved two-to-two stripping tower 2 and the improved three-to-three stripping tower 3 are reduced, the operation working condition and the operation are relatively optimized, the steam consumption is reduced, other parts are treated by the ammonia recovery device, the operation loads of the three sets of conversion stripping towers and the operation load of the ammonia recovery device can be flexibly adjusted according to the operation requirement, on one hand, the treatment capacity of the conversion stripping towers is reduced, and the system corrosion is reduced; on the other hand, the transform condensate after ammonia recovery unit handles can realize the ammonia separation of acid gas and, and the ammonia product is purer, and the gaseous ammonia of output high-purity and the aqueous ammonia of different concentrations have solved boiler desulfurization system water balance and ammonia balance problem, also improve the quality of ammonium sulfate greatly, and the partial gaseous ammonia of output supplies the boiler to sell the use, fine satisfied boiler desulfurization denitration's use.
Because the ammonia gas enriched in the middle of the stripping tower 6 exists in the presence of carbon dioxide, ammonia and water vapor, ammonium salt crystals can be generated if the ammonia gas is obtained through one-time cooling, the recovery rate of ammonia is influenced, and meanwhile, the generated ammonium salt crystals block equipment and pipelines. Therefore, the separation of ammonia and carbon dioxide is carried out by successively reducing the temperature and the pressure, namely, the separation is carried out by the three-stage partial condenser 7.
The bottom of the three-stage partial condenser 7 is connected with a raw material water tank 5 for retreatment.
Because the crude ammonia gas on the upper part of the three-stage partial condenser 7 also has partial acid gas, further desulfurization and decarburization are needed, the refining tower 8 is divided into two sections, more than 95 percent of carbon dioxide and hydrogen sulfide are removed in the lower section, and the solution is circularly absorbed; and the upper section uses fresh low-temperature concentrated ammonia water to deeply remove the residual carbon dioxide and hydrogen sulfide.
Preferably, the upper gas phase outlet of the refining tower 8 is used for connecting with a user.
The refining tower 8 is connected with an ammonia water preparation device 9 for preparing ammonia water with different concentrations, and the ammonia desulphurization method or the ammonia sales method of a boiler of a user is determined according to the process requirements or the user requirements. The middle part of the stripping tower is led out a pipeline to be connected with a partial condenser which is connected with a refining tower, the refining tower is subjected to desulfurization and decarburization once more to produce high-purity gas ammonia, the gas ammonia enters a flue gas SCR denitration device and an ammonia water taking device, strong ammonia water is circularly prepared, the strong ammonia water is used for ammonia desulfurization all the way, and ammonia water storage tanks are circularly prepared all the way, so that the ammonia water with different concentrations can be taken out.
The embodiment provides a condensate conversion treatment method, which comprises the following steps: the shift low-temperature condensate is converted into sulfur-containing low-concentration ammonia water through a shift stripping tower, the sulfur-containing low-concentration ammonia water is used for ammonia desulphurization, and the number of the shift stripping towers is at least two; according to the operation condition, selecting part or all of low-temperature condensate to enter an ammonia recovery device without a transformation stripping tower for purification and then using the condensate for ammonia desulphurization; according to the operation condition, part or all of the sulfur-containing low-concentration ammonia water is selected to enter an ammonia recovery device for purification and then is used for ammonia desulphurization.
Through testing, the pure ammonia amount delivered by the ammonia recovery device is 823kg/h, 6584 tons of liquid ammonia are purchased each year, 48 tons of liquid ammonia are supplemented each year by deducting the index fluctuation of boiler operation tail gas, and 6536 tons of liquid ammonia are purchased each year; according to the same unified calculation standard, namely liquid ammonia is 3465 yuan/ton, the liquid ammonia purchasing cost is reduced by 2264.72 ten thousand yuan per year, the operation cost is reduced by 451.89 ten thousand yuan per year, and the expected benefit is 1812.83 ten thousand yuan per year. The unit price of the ammonium sulfate product is improved by 40 yuan/ton after the quality of the ammonium sulfate product is improved, and according to the average yield of 60 tons/day, the product benefit is improved by 79.2 ten thousand yuan/year according to the improvement of the product quality; the sum of the two results in the benefit of 1892.03 ten thousand yuan per year.
In the prior art, transformation low-temperature condensation can only be processed through respective transformation stripping towers, sulfur-containing low-concentration ammonia water is delivered to a boiler for ammonia desulphurization, the operation load of the condensate stripping tower is influenced by the process and the technology, the corrosion is high, the impurities such as acid gas components and metal ions in the produced sulfur-containing low-concentration ammonia water are high, the water balance desulphurization effect of a desulphurization system is seriously influenced, the ammonia balance of the system is difficult to realize, secondary pollution and resource waste caused by ammonia escape are formed, the quality of byproducts such as ammonium sulfate is poor, and the stable operation of the boiler desulphurization system is influenced. The invention realizes the free distribution of the low-temperature condensate by three sets of conversion according to the operating condition of the condensate stripping tower, reduces the treatment capacity of the conversion condensate stripping tower, solves the problem that a single set of conversion stripping tower cannot exit, realizes the flexible operation of the conversion condensate system, and saves the starting and stopping cost by 10 ten thousand times. Simultaneously ammonia recovery unit is through the optimal combination to low temperature condensate and the dilute aqueous ammonia that contains sulphur, realized will transform condensate purification treatment, the gaseous ammonia of output high-purity and the aqueous ammonia of different concentrations, boiler desulfurization system water balance and ammonia balance problem have been solved, also improve the quality of ammonium sulfate greatly, the part gaseous ammonia of output supplies the boiler to sell off the use, the cost of boiler purchase liquid ammonia has been reduced, the aqueous ammonia is made to surplus ammonia and is sold simultaneously, greatly reduced manufacturing cost, system steady operation has been satisfied.
No matter what kind of mode is adopted to improve the conversion condensate treatment pipeline and the process, the same effect can be realized as long as three sets of conversion condensate can correspond to different treatment modes and flexible conversion is realized finally.
Although the embodiments of the present invention have been described with reference to the accompanying drawings, it is not intended to limit the scope of the invention, and it should be understood by those skilled in the art that various modifications and variations can be made without inventive changes in the technical solutions of the present invention.
Claims (10)
1. A shift condensate treatment system, comprising: at least two shift stripper columns and an ammonia recovery unit;
the inlets of the two shift stripping towers are respectively connected with a shift low-temperature condensate pipeline, the outlets of the two shift stripping towers are sulfur-containing low-concentrated ammonia water pipelines, the two shift low-temperature condensate pipelines are respectively provided with a first pipeline connected to the inlet of the ammonia recovery device, the sulfur-containing low-concentrated ammonia water pipeline is provided with a second pipeline connected to the inlet of the ammonia recovery device, the outlet of the ammonia recovery device is connected to the sulfur-containing low-concentrated ammonia water pipeline through a third pipeline, and the sulfur-containing low-concentrated ammonia water pipeline is used for being connected to boiler ammonia desulphurization equipment.
2. The shift condensate treatment system according to claim 1, wherein the low concentrated ammonia containing water line is provided with three ammonia water towers, and the outlets of the three shift strippers are connected to the ammonia water towers.
3. The shift condensate treatment system according to claim 1, wherein the ammonia recovery unit comprises a stripper having a shift condensate inlet in a middle portion thereof, the shift condensate inlet corresponding to the plurality of shift condensate lines, the stripper having an acid gas vent line at a top portion thereof and a purified water vent line at a bottom portion thereof.
4. The shift condensate treatment system according to claim 3, wherein the ammonia recovery unit further comprises a three-stage dephlegmator, and wherein the stripper mid-column outlet line is connected to the three-stage dephlegmator.
5. The shift condensate treatment system according to claim 4, wherein the ammonia recovery unit further comprises a raw water tank, the bottom of the three stage dephlegmator being connected to the raw water tank.
6. The shift condensate treatment system according to claim 4, wherein the ammonia recovery unit further comprises a refining tower, the upper part of the three-stage partial condenser is connected with the refining tower, the refining tower is divided into two sections, at least 95% of carbon dioxide and hydrogen sulfide are removed in the lower section, and the solution is circularly absorbed; and the upper section uses fresh low-temperature concentrated ammonia water to deeply remove the residual carbon dioxide and hydrogen sulfide.
7. The shift conversion condensate treatment system according to claim 6, wherein the ammonia recovery unit further comprises an ammonia water preparation device, the pipeline led out from the top of the refining tower is connected with the ammonia water preparation device, and the ammonia water preparation device is used for preparing different strong ammonia water.
8. A method of shift condensate treatment, comprising:
the shift low-temperature condensate is converted into sulfur-containing low-concentration ammonia water through a shift stripping tower, the sulfur-containing low-concentration ammonia water is used for ammonia desulphurization, and the number of the shift stripping towers is at least two;
according to the operation condition, selecting part or all of low-temperature condensate to enter an ammonia recovery device without a transformation stripping tower for purification and then using the condensate for ammonia desulphurization;
according to the operation condition, selecting partial or all sulfur-containing low-concentration ammonia water to enter an ammonia recovery device for purification and then using for ammonia desulphurization.
9. The shift condensate treatment process of claim 8, wherein the ammonia recovery unit purge comprises: the conversion condensate enters a stripping tower, rich ammonia gas with part of acid gas removed is extracted from the middle part of the stripping tower and enters a three-stage partial condenser, crude ammonia gas is obtained at the top after further separation with the acid gas in the three-stage partial condenser and enters a refining tower, and the acid gas is deeply removed in the refining tower.
10. The shift condensate treatment method according to claim 9, wherein the ammonia gas refined in the refining tower is sent to an ammonia water preparation device, and the ammonia water prepared by the ammonia water preparation device is sent to a boiler for ammonia desulfurization or ammonia water sale.
Priority Applications (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| 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 |
| AU2023296338A AU2023296338B2 (en) | 2022-07-18 | 2023-07-17 | Shift condensate treatment system and process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210842707.1A CN115259259B (en) | 2022-07-18 | 2022-07-18 | System and process for treating conversion condensate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115259259A true CN115259259A (en) | 2022-11-01 |
| CN115259259B CN115259259B (en) | 2023-06-16 |
Family
ID=83767866
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210842707.1A Active CN115259259B (en) | 2022-07-18 | 2022-07-18 | System and process for treating conversion condensate |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN115259259B (en) |
| AU (1) | AU2023296338B2 (en) |
| WO (1) | WO2024017202A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024017202A1 (en) * | 2022-07-18 | 2024-01-25 | 陕西未来能源化工有限公司 | Shift condensate treatment system and process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130092026A1 (en) * | 2011-10-18 | 2013-04-18 | Alstom Technology Ltd. | 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 |
| CN106582272A (en) * | 2016-12-14 | 2017-04-26 | 山东迅达化工集团有限公司 | Desulfuration purification process for acidic waste water steam stripping ammonia gas |
| 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 |
| CN110203986A (en) * | 2019-05-16 | 2019-09-06 | 中国神华煤制油化工有限公司 | The method for reducing the system of ammonia-nitrogen content and reducing ammonia-nitrogen content |
| 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 |
Family Cites Families (4)
| 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. |
| 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 |
| 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 |
-
2022
- 2022-07-18 CN CN202210842707.1A patent/CN115259259B/en active Active
-
2023
- 2023-07-17 AU AU2023296338A patent/AU2023296338B2/en active Active
- 2023-07-17 WO PCT/CN2023/107744 patent/WO2024017202A1/en active Application Filing
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20130092026A1 (en) * | 2011-10-18 | 2013-04-18 | Alstom Technology Ltd. | 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 |
| CN106582272A (en) * | 2016-12-14 | 2017-04-26 | 山东迅达化工集团有限公司 | Desulfuration purification process for acidic waste water steam stripping ammonia gas |
| 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 |
| CN110203986A (en) * | 2019-05-16 | 2019-09-06 | 中国神华煤制油化工有限公司 | The method for reducing the system of ammonia-nitrogen content and reducing ammonia-nitrogen content |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2024017202A1 (en) * | 2022-07-18 | 2024-01-25 | 陕西未来能源化工有限公司 | Shift condensate treatment system and process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115259259B (en) | 2023-06-16 |
| AU2023296338B2 (en) | 2024-06-27 |
| WO2024017202A1 (en) | 2024-01-25 |
| AU2023296338A1 (en) | 2024-02-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110040691B (en) | Device and method for preparing and producing high-purity sulfur dioxide by using acid gas | |
| CN115259259A (en) | Conversion condensate treatment system and process | |
| CN105521687A (en) | Method for by-producing sulphur from hydrogen sulfide gas produced during hydrogenation of coal tar | |
| CN100579896C (en) | Method and system for preparing synthetic gas with appropriate hydrogen-carbon ratio from lurgi furnace outlet coal gas through non-catalytic partial oxidation by pure oxygen | |
| CN104030514B (en) | A kind of processing method of dual-effect energy-saving wastewater stripping depickling deamination | |
| CN106457137A (en) | Systems and methods for enhanced separation of hydrogen sulfide and ammonia in hydrogen sulfide stripper | |
| CN104098069B (en) | A kind of coal gas carries the device of hydrogen | |
| CN209854029U (en) | Device for preparing methanol from synthesis gas without conversion system | |
| CN210103457U (en) | Device for preparing and producing high-purity sulfur dioxide by utilizing acid gas | |
| CN112374459A (en) | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery | |
| CN219058554U (en) | Multi-level high-purity nitric acid co-production system | |
| CN213433047U (en) | Single-tower open type steam stripping device for acid water conversion treatment | |
| CN216986990U (en) | High-efficiency energy-saving regeneration device for recycling low-temperature methanol washing carbon dioxide in grading manner | |
| CN214829037U (en) | Device for producing dilute nitric acid by magnesium nitrate method | |
| CN215027472U (en) | By using a gas containing SO3Device for increasing conventional concentration sulfuric acid concentration by using dry flue gas | |
| CN211677111U (en) | Viscose waste gas treatment recovery plant | |
| CN210645772U (en) | Produce acid gas purifier of multiple purity hydrogen sulfide | |
| CN103407971A (en) | Novel technology for production of liquid sulfur dioxide | |
| CN209668781U (en) | The system of lighter hydrocarbons impurity in a kind of novel carbon dioxide removal | |
| CN206955651U (en) | System for recovering waste hydrogen of oil refinery for ammonia synthesis device of chemical fertilizer plant | |
| CN107998689B (en) | Removing CO in the medium-to-variable gas acidic condensate2And O2Heat integrated rectification process | |
| CN220003002U (en) | Single-tower closed steam stripping device for acid water conversion treatment | |
| EP0214734B1 (en) | Method and apparatus for making sulphuric acid | |
| CN110548370A (en) | Acid gas purification process and device for producing hydrogen sulfide with various purities | |
| CN205773852U (en) | Phenol ammonia waste water processing and utilizing system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |