CN107697931B - Multistage reverse circulation ammonia absorption process - Google Patents
Multistage reverse circulation ammonia absorption process Download PDFInfo
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- CN107697931B CN107697931B CN201711055534.4A CN201711055534A CN107697931B CN 107697931 B CN107697931 B CN 107697931B CN 201711055534 A CN201711055534 A CN 201711055534A CN 107697931 B CN107697931 B CN 107697931B
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- 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
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G9/00—Compounds of zinc
- C01G9/02—Oxides; Hydroxides
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The invention discloses a multistage circulation reverse ammonia absorption process, which comprises a simultaneous multistage ammonia absorption circulation section. The ammonia absorption circulation of each level is divided into 1, 2.. N levels of ammonia absorption circulation from high to low according to the concentration of ammonia absorption liquid, the ammonia-containing mixed gas to be absorbed flows through 1 to N levels of ammonia absorption circulation sections in sequence, the gas is absorbed by the ammonia absorption liquid with higher ammonia concentration, the gas which is not completely absorbed enters the adjacent lower level of ammonia absorption circulation section, and the gas is absorbed by the ammonia absorption liquid with lower ammonia concentration. The ammonia absorption liquid in each stage of ammonia absorption circulation section respectively flows back to the ammonia circulation tanks of the stage and the adjacent upper stage to be used as the supplement liquid of the ammonia absorption liquid, wherein the N-stage ammonia absorption liquid is directly supplemented by the external ammonia absorption liquid, and the ammonia absorption liquid with ammonia concentration reaching a specified value in the 1-stage ammonia absorption circulation section is subjected to heat exchange treatment with controllable strength, so that the automatic continuous output of the ammonia water recycling liquid with qualified concentration and higher temperature is realized, and the ammonia water recycling liquid has the characteristics of high ammonia absorption rate, simplicity in operation, energy conservation and consumption reduction.
Description
Technical Field
The invention relates to an ammonia gas absorption method in an ammonia distillation process, in particular to a multistage reverse circulation ammonia absorption process method in an ammonia-process zinc oxide process.
Background
The technological process of ammonia-process zinc oxide is an ammonia circulation process, ammonia water is used for complexing zinc, the evaporated ammonia is used for crystallizing zinc ions, and the ammonia gas of the evaporated ammonia can be used for complexing zinc as a zinc-ammonia complexing solution after being converted into the ammonia water through ammonia absorption. The maximum energy consumption of the ammonia-process zinc oxide process is steam used for ammonia distillation, and in a high-efficiency ammonia distillation device, the steam energy consumed by heating the zinc ammine complex liquid from normal temperature to boiling accounts for 50% of the evaporation amount of the whole process.
In the traditional ammonia-method zinc oxide process, a high-level ammonia absorber is mainly adopted to absorb ammonia gas, in order to ensure the sufficient absorption of the ammonia gas, ammonia absorption liquid needs to be sufficiently cooled in a cold discharge mode and the like, and the cooled ammonia absorption liquid is subjected to process circulation ammonia absorption again. And when the final ammonia absorption solution with the ammonia concentration reaching the qualified value is used as an ammonia water stock solution in the zinc ammine complex solution, the zinc ammine complex solution is boiled in a steam heating mode in the ammonia distillation process after the complex reaction, so that the zinc ammine complex solution is heated from the normal temperature to the heat consumption in the boiling process again.
In addition, a fractional liquid-transferring mode is adopted in the traditional ammonia absorption process of the high-level ammonia absorber, after the absorption liquid absorbs ammonia repeatedly and circularly, the ammonia concentration in the ammonia absorption liquid in the circulating tank is gradually increased until the ammonia concentration in the absorption liquid is qualified through manual inspection, the absorption liquid is transferred out in a fractional manner, circulating water is supplemented in a fractional manner, and then ammonia absorption is continued. According to the traditional ammonia absorption mode of the high-level ammonia absorber, ammonia is well absorbed when ammonia absorption liquid in the circulating tank is at low concentration, and the problem of insufficient ammonia absorption exists when the concentration is high; when qualified ammonia water is transferred out in a graded manner to absorb ammonia liquid, the interruption of the ammonia absorption process of the whole high-level ammonia absorption system is caused, and the ammonia absorption efficiency is low; and the whole traditional high-level ammonia absorber ammonia absorption process can be completed without manual operation and guard such as ammonia water concentration detection, liquid conversion in different times, cyclic water supplement in different times and the like, and the process cost is high.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, provides a multistage reverse circulation ammonia absorption process, and solves the problems of heat waste, insufficient ammonia absorption, high process cost and low working efficiency of fractional transfer in the traditional high-level ammonia absorption method.
In order to achieve the above purpose, the invention provides the following technical scheme:
a multi-stage reverse circulation ammonia absorption process comprises N stages of ammonia absorption circulation which are carried out simultaneously, wherein
Each stage of ammonia absorption cycle is divided into 1 and 2.
The ammonia-containing mixed gas flows through the 1-N-stage ammonia absorption circulation section in sequence, is subjected to reverse circulation absorption, and is absorbed by the ammonia absorption liquid with higher concentration and then absorbed by the ammonia absorption liquid with lower concentration;
when the ammonia concentration of the ammonia absorption liquid in the 1 st stage of ammonia absorption cycle reaches a preset value, outputting the ammonia as a product;
meanwhile, in order to ensure the stability of the concentration of the ammonia absorption liquid in each level of ammonia absorption circulation section, the ammonia absorption liquid in the m levels of ammonia absorption circulation sections is used as a make-up liquid and flows into the m +1 levels of ammonia absorption circulation sections in a flow-controllable manner; wherein m is more than or equal to 1 and less than or equal to N; and the make-up liquid of the ammonia absorption liquid in the N-stage ammonia absorption circulation section is directly provided by the external ammonia absorption liquid.
According to the technical scheme, the ammonia-containing mixed gas generated in the ammonia distillation process sequentially flows through the 1-N stages of ammonia absorption circulation sections by reversing the existing ammonia absorption sequence, and is reversely and circularly absorbed by the ammonia absorption liquid in each stage of ammonia absorption circulation section, and the method specifically comprises the following steps: the high concentration of earlier by in the 1 st level inhale ammonia liquid and absorb the back, absorb by the lower concentration inhale ammonia liquid in proper order again to effectively improve the ammonia absorption rate, effectively prevent at multistage ammonia absorption in-process, when later stage high concentration inhales ammonia liquid and absorbs, absorb exothermic temperature rise that leads to, cause the ammonia to absorb inadequately even the ammonia is excessive. And through adjusting the concentration parameters of the ammonia absorption liquid in the ammonia absorption circulation sections of all the stages and the flow of the make-up liquid between all the stages, the automatic circulation of the whole multistage reverse circulation ammonia absorption can be realized, and the continuous output of ammonia-containing liquid products with qualified concentration in the 1 st-stage ammonia absorption circulation section can be realized, so that the multistage automatic circulation absorption and output of high ammonia gas absorption rate can be realized, the ammonia gas absorption process efficiency is effectively improved, and the ammonia absorption process cost is reduced.
By taking the ammonia absorption liquid in each stage of ammonia absorption circulation section as a make-up liquid, the ammonia absorption liquid is divided into two flows of ammonia absorption circulation sections with lower concentration
As a preferable embodiment of the present invention, the ammonia absorption method comprises N stages of ammonia absorption cycles performed simultaneously as follows:
(1) primary ammonia absorption: pumping the primary ammonia absorption liquid in the primary ammonia circulation tank into a primary ammonia absorber through a water pump, carrying out gas-liquid mixing ammonia absorption on the primary ammonia absorber and the ammonia absorption mixed gas to be absorbed introduced into the primary ammonia absorber from the outside, carrying out heat exchange treatment on ammonia water after ammonia absorption through a primary heat exchanger, and refluxing a part of ammonia water into the primary ammonia circulation tank to continuously absorb ammonia in a circulating manner;
the other part of ammonia absorption liquid with the ammonia concentration reaching the preset value range is taken as a product of the ammonia absorption process and flows back to the qualified ammonia water storage tank so as to be transferred and output;
(2) secondary ammonia absorption: pumping the secondary ammonia absorption liquid in the secondary ammonia circulation tank into a secondary ammonia absorber through a water pump, further carrying out gas-liquid mixing ammonia absorption with the ammonia-containing mixed gas which is not completely absorbed in the primary ammonia absorber, carrying out heat exchange treatment on ammonia water after ammonia absorption through a secondary heat exchanger, and refluxing a part of ammonia water to the secondary ammonia circulation tank for continuous ammonia absorption in a circulating manner;
the other part of the ammonia liquid flows back to the primary ammonia circulating tank to be used as a supplementary liquid of the primary ammonia absorption liquid;
(3) three-stage ammonia absorption: pumping the tertiary ammonia absorption liquid in the tertiary ammonia circulation tank into a tertiary ammonia absorber through a water pump, carrying out further gas-liquid mixing ammonia absorption with the ammonia-containing mixed gas which is not completely absorbed in the secondary ammonia absorber, and refluxing a part of ammonia water after ammonia absorption into the tertiary ammonia circulation tank to continuously circularly absorb ammonia after heat exchange treatment;
the other part of the ammonia flows back into a secondary ammonia circulating tank to be used as a supplementary liquid of secondary ammonia absorption liquid;
………
(4) n-stage ammonia absorption: pumping N-grade ammonia absorption liquid in the N-grade ammonia circulation tank into the N-grade ammonia absorber through a water pump, further carrying out gas-liquid mixing ammonia absorption with ammonia-containing mixed gas which is not completely absorbed in the N-1-grade ammonia absorber, and refluxing a part of ammonia water after ammonia absorption into the N-grade ammonia circulation tank to continuously circularly absorb ammonia after heat exchange treatment;
the other part of the ammonia flows back into the N-1-level ammonia circulating tank to be used as a supplementary liquid of the N-1-level ammonia absorbing liquid;
the absorption liquid in the N-stage circulation tank is directly supplemented by external ammonia absorption liquid;
the ammonia concentration in each level of ammonia absorption liquid is gradually decreased from one level to N levels, wherein the concentration of the ammonia absorption liquid at one level is the highest, and the concentration of the ammonia absorption liquid at N levels is the lowest.
In another preferred embodiment of the present invention, the value of N is specifically 3.
As a further preferable scheme of the present invention, valves are arranged in the communication pipelines between the ammonia absorbers at each stage and the corresponding ammonia circulation tanks or ammonia storage tanks, and the flow rate of the ammonia absorbing liquid flowing back to each ammonia circulation tank or ammonia storage tank is adjusted, so that the effective control of the ammonia concentration of the qualified ammonia water transferred out finally is realized.
As a further preferable scheme of the invention, a heat exchanger capable of controlling the flow of external cold substances is connected between the primary ammonia absorber and the ammonia storage tank, so that the temperature of the qualified ammonia water flowing back to the ammonia storage tank is controlled. The heat exchanger of controllable outer cold matter flow makes the high concentration/protection aqueous ammonia solution of foremost ammonia absorption tower monomer backward flow can carry out the heat transfer according to anticipated heat transfer intensity, and then makes the temperature of the liquid in the ammonia storage tank can control the adjustment, can practice thrift the heat input when the aqueous ammonia solution that utilizes these refluxes carries out other reactions, for example when being used for ammonia method zinc dipping with the aqueous ammonia in the ammonia storage tank, the heating strength of reaction liquid is showing and is reducing.
As a preferable mode of the further step of the present invention, a flow meter is connected to the absorption liquid input point. The flow meter monitors the running state of the ammonia absorption device system, so that the total amount of the absorption liquid in the system can be controlled within a stable range, and the integral stable running of the system is ensured. Can make the efficiency of inhaling ammonia higher, the aqueous ammonia concentration of output is more stable, more is close expected value.
As a further preferable scheme of the invention, the inlet of the ammonia storage tank is provided with a flow meter. The flow meter monitors the running state of the ammonia absorption device system, so that the total amount of the absorption liquid in the system can be controlled within a stable range, and the integral stable running of the system is ensured. Can make the efficiency of inhaling ammonia higher, the aqueous ammonia concentration of output is more stable, more is close expected value. Especially, the flowmeter is arranged at the inlet of the ammonia storage tank and the absorption liquid supplement interface, and the two flowmeters can effectively monitor the liquid inlet and outlet of the ammonia absorption device system, so that the stable operation of the system is realized.
Compared with the prior art, the invention has the beneficial effects that:
(1) in the ammonia gas absorption method, the ammonia-containing mixed gas generated in the external ammonia distillation process is firstly mixed and absorbed by the ammonia gas absorption liquid with higher concentration in the primary ammonia absorption cycle process section; the incompletely absorbed ammonia gas enters an adjacent lower-level ammonia absorption cycle section, and is further mixed and absorbed by ammonia absorption liquid with lower concentration, so that the graded countercurrent cycle absorption of ammonia-containing mixed gas is realized, the ammonia gas absorption rate is improved, and the process cost is reduced.
(2) Ammonia gas in each stage of ammonia absorber absorbs liquid, and a part of the ammonia gas reflows to an ammonia absorbing circulating tank which provides absorption liquid for the monomer at the stage and is used as the absorption liquid to continue circulating absorption; the other part of the ammonia liquid flows back to an adjacent lower ammonia absorption circulating tank to be used as supplement of the absorption liquid with adjacent concentration. The whole ammonia absorption circulating system is in a closed circulating state, flow control valves can be installed on all backflow branches, and flow meters for detecting outflow flow of qualified ammonia water and input flow of external process circulating water are matched with each other for use, so that automatic continuous outflow of the qualified ammonia absorption liquid with controllable concentration is realized, the difficulty of process operation is reduced, the problems of assay in repeated transfer in ammonia absorption operation of a traditional high-level ammonia absorber, transfer of the qualified ammonia water and transfer of the operation of circulating water for ammonia absorption are solved, an unattended mode can be realized in practical application, the process efficiency is improved, the labor cost is saved, and meanwhile, the environmental problem caused by ammonia volatilization is effectively solved.
(3) The temperature of the ammonia absorption recovery liquid with qualified concentration is controlled by adjusting the flow of the external cooling material in the controllable external cooling material flow heat exchanger. The ammonia absorption recovery liquid can save heat input when carrying out other reactions, for example, when the ammonia absorption recovery liquid is continuously used as ammonia water stock solution for complexing of zinc ions, the saving amount of process steam can reach 30-40%.
Drawings
FIG. 1 is a process flow diagram of the ammonia absorption method of the present invention.
FIG. 2 is a schematic structural view of an ammonia absorption device according to the present invention.
Wherein: a primary ammonia absorption monomer 1, a secondary ammonia absorption monomer 2, a tertiary ammonia absorption monomer 3, a tertiary ammonia absorption heat exchanger 4, a secondary ammonia absorption heat exchanger 5, a primary ammonia absorption heat exchanger 6, a controllable external cooling water flow heat exchanger 7, a flowmeter I8, an ammonia storage tank 9, a primary ammonia absorption circulation tank 10, a secondary ammonia absorption circulation tank 11, a tertiary ammonia absorption circulation tank 12, an external process circulation water tank and inlet 13, a flowmeter II 14, a primary process water pump 15, a secondary process water pump 16, a tertiary process water pump 17, a primary ammonia inlet 101, a primary ammonia distributor 102, a primary absorption liquid inlet 103, a primary absorption liquid spray head 104, a primary ammonia outlet 105, a secondary ammonia inlet 201, a secondary ammonia distributor 202, a secondary absorption liquid inlet 203, a secondary absorption liquid spray head 204, a secondary ammonia outlet 205, a tertiary ammonia inlet 301, a tertiary ammonia distributor 302, a tertiary absorption liquid inlet 303, the three-stage absorption liquid spray head 304, a first valve 601, a second valve 701, a third valve 1001, a fourth valve 1101, a fifth valve 1102 and a sixth valve 1201.
DETAILED DESCRIPTION OF EMBODIMENT (S) OF INVENTION
The invention is further described in detail by taking an ammonia absorption process method consisting of 3 stages of ammonia absorption cycles as an example and combining an ammonia absorption device for implementing the ammonia absorption method and corresponding drawings. It should be understood that the scope of the above-described subject matter is not limited to the following examples, and any techniques implemented based on the disclosure of the present invention are within the scope of the present invention.
When n is 3 as shown in fig. 1, the ammonia gas absorption method of the present invention includes a three-stage ammonia absorption cycle process section which is in a simultaneous state when the ammonia absorption device is in normal use.
(1) Primary ammonia absorption: pumping the primary absorption liquid in the primary ammonia circulation tank into a primary ammonia absorber through a water pump, carrying out gas-liquid mixing with external ammonia-containing mixed gas introduced into the primary ammonia absorber to absorb ammonia, carrying out heat exchange treatment on ammonia water after ammonia absorption through a primary heat exchanger, and refluxing a part of ammonia water to enter the primary ammonia circulation tank to continuously absorb ammonia in a circulating manner; and the other part of ammonia absorption liquid with the concentration reaching the preset value range is taken as a product of the ammonia absorption process, flows back to the qualified ammonia water storage tank and is transferred and output as the product.
(2) Secondary ammonia absorption: pumping the secondary absorption liquid in the secondary ammonia circulating tank into a secondary ammonia absorber through a water pump, further carrying out gas-liquid mixing ammonia absorption with the ammonia-containing mixed gas which is not completely absorbed in the primary ammonia absorber, carrying out heat exchange treatment on ammonia water after ammonia absorption by a secondary heat exchanger, and refluxing a part of ammonia water into the secondary ammonia circulating tank to continuously circularly absorb ammonia; the other part of the ammonia flows back to the primary ammonia circulating tank to be used as a supplementary liquid of the primary absorption liquid;
(3) three-stage ammonia absorption: pumping the tertiary absorption liquid in the tertiary ammonia circulation tank into a tertiary ammonia absorber through a water pump, carrying out further gas-liquid mixing ammonia absorption with the ammonia-containing mixed gas which is not completely absorbed in the secondary ammonia absorber, and refluxing a part of ammonia water after ammonia absorption into the tertiary ammonia circulation tank to continuously circularly absorb ammonia after heat exchange treatment; the other part of the ammonia flows back into a secondary ammonia circulating tank to be used as a supplementary liquid of a secondary absorption liquid; the absorption liquid in the 3-stage circulation tank is directly supplemented by external absorption liquid;
the ammonia-containing concentration in each stage of absorption liquid is gradually decreased from one stage to three stages, wherein the concentration of the first stage absorption liquid is the highest, and the concentration of the third stage absorption liquid is the lowest.
The following will further describe in detail the specific operation steps of the ammonia gas absorption method composed of 3 stages of ammonia absorption cycles with the ammonia absorption device of the present invention.
As shown in fig. 2, the novel ammonia gas absorbing apparatus (ammonia absorbing apparatus) comprises: the ammonia absorption device comprises a multi-stage ammonia absorption tower, a heat exchanger, an ammonia absorption circulating tank, a process water pump and an ammonia storage tank, wherein the components are mutually communicated through a process pipeline to form a closed circulating system. The multistage ammonia absorption tower comprises a three-stage ammonia absorption tower monomer, namely a first-stage ammonia absorption tower monomer 1, a second-stage ammonia absorption tower monomer 2 and a third-stage ammonia absorption tower monomer 3 from bottom to top; the heat exchanger comprises a primary ammonia absorption heat exchanger 4, a secondary ammonia absorption heat exchanger 5, a tertiary ammonia absorption heat exchanger 6 and a controllable external cooling water flow heat exchanger 7; the ammonia absorption circulating tank comprises a first-stage ammonia absorption circulating tank 10, a second-stage ammonia absorption circulating tank 11 and a third-stage ammonia absorption circulating tank 12; the process water pumps comprise a first-stage process water pump 15, a second-stage process water pump 16 and a third-stage process water pump 17.
The lower part of the first-stage ammonia absorption tower monomer is provided with a first-stage ammonia gas inlet 101 and a first-stage ammonia gas distributor 102 which are used for receiving and diffusing ammonia-containing mixed gas generated in an external ammonia distillation process; the upper part of the first-stage ammonia absorption tower monomer is provided with a first-stage ammonia outlet 105 which is communicated with a second-stage ammonia inlet 201 positioned at the lower part of the second-stage ammonia absorption tower monomer 2; the upper part of the second-stage ammonia absorption monomer is provided with a second-stage ammonia outlet 205 which is communicated with a third-stage ammonia inlet 301 positioned at the lower part of the third-stage ammonia absorption monomer, and the third-stage ammonia absorption monomer is not provided with an ammonia outlet, so that the externally received ammonia-containing mixed gas can sequentially flow through each ammonia absorption tower monomer.
And the upper part or the top of each stage of ammonia absorption tower monomer is provided with an ammonia absorption liquid inlet, one end of the absorption liquid inlet is connected with a corresponding absorption liquid spray head, and the other end of the absorption liquid inlet is sequentially communicated with each stage of process water pump and each ammonia absorption circulating tank, so that the absorption liquid in each stage of circulating tank can be pumped into each stage of ammonia absorption monomer through the water pump, the input of the absorption liquid is realized, the input absorption liquid is sprayed through the absorption liquid spray head, and the contact area between the absorption liquid and the mixed gas is enlarged. Wherein, a primary absorption liquid inlet 103 is arranged at the upper part of the primary ammonia absorption monomer, one end of the primary absorption liquid inlet is connected with a primary absorption liquid spray head 104, and the other end is sequentially connected with a primary process water pump 15 and a primary ammonia absorption circulating tank 10 in series; a secondary absorption liquid inlet 203 is arranged at the upper part of the secondary ammonia absorption monomer, one end of the secondary absorption liquid inlet is connected with a secondary absorption liquid spray head 204, and the other end is sequentially connected with a secondary process water pump 16 and a secondary ammonia absorption circulating tank 11 in series; and a third-stage absorption liquid inlet 303 is arranged at the top of the third-stage ammonia absorption monomer, one end of the third-stage absorption liquid inlet is connected with a third-stage absorption liquid spray head 304, and the other end of the third-stage absorption liquid inlet is sequentially connected with a third-stage process water pump 17 and a third-stage ammonia absorption circulation tank 12 in series.
An ammonia absorption liquid return pipeline is arranged at the bottom of each level of ammonia absorption tower monomer, wherein ammonia absorption liquid formed by gas-liquid mixing absorption of high-concentration absorption liquid in the first level of ammonia absorption tower monomer 10 and external ammonia-containing mixed gas is divided into two branches through the return pipeline, part of ammonia absorption liquid reaching qualified concentration flows back to the ammonia storage tank 9 after heat exchange treatment of the controllable external cold water flow heat exchanger 7, and a valve II 701 is further arranged on each branch and used for controlling the flow of ammonia absorption liquid flowing back to the ammonia storage tank 9; and the other part of ammonia absorption liquid is subjected to heat exchange treatment by the primary ammonia absorption heat exchanger 6 and then flows back to the primary ammonia absorption circulating tank 10 to be used as absorption liquid, ammonia-containing mixed gas is continuously and circularly absorbed, and the flow of the ammonia absorption liquid of the branch is controlled by a first valve 601.
The medium-concentration absorption liquid in the secondary ammonia absorption circulating tank 11 is input into the secondary ammonia absorption monomer through a secondary process water pump 16, is further subjected to gas-liquid mixing absorption with the ammonia-containing mixed gas which is not absorbed in the primary ammonia absorption tower monomer 1, the ammonia absorption liquid formed after ammonia absorption is subjected to heat exchange treatment by a secondary ammonia absorption heat exchanger 5, a part of the ammonia absorption liquid flows back to the primary ammonia absorption circulating tank 10 to be used as a supplement liquid of the ammonia absorption liquid, and the reflux flow of the branch is controlled by a valve III 1001; the other part of the ammonia gas returns to the secondary ammonia absorption circulation tank 11 to be used as absorption liquid to continuously absorb the ammonia-containing mixed gas in a circulating way, and the return flow is controlled by a valve IV 1101.
The low-concentration absorption liquid in the three-stage ammonia absorption circulating tank 12 is pumped into the three-stage ammonia absorption tower monomer 3 through the three-stage process water pump 12, is further subjected to gas-liquid mixing absorption with the ammonia-containing mixed gas which is not absorbed in the two-stage ammonia absorption monomer 2, the ammonia absorption liquid formed after ammonia absorption is subjected to heat exchange treatment through the three-stage ammonia absorption heat exchanger 4, one part of the ammonia absorption liquid flows back into the two-stage ammonia absorption circulating tank 11 to serve as ammonia absorption liquid replenishing liquid, the other part of the ammonia absorption liquid flows back into the three-stage ammonia absorption circulating tank 12, and the flow of the backflow branch is controlled through a valve five 1102 and a valve six 1201 respectively. The bottom of the three-stage ammonia absorption circulating tank 12 is communicated with external process circulating water 13 and is used for supplementing the external process water.
A first flowmeter 8 is arranged at an inlet of the ammonia storage tank 9 and used for detecting the flow of ammonia absorption liquid flowing back to the ammonia storage tank; a second flowmeter 14 is arranged at the external process circulating water inlet and is used for detecting the flow of external process circulating water input into the ammonia absorption circulating system; the first flow meter 8 and the second flow meter 14 are matched with valves for controlling the flow of the ammonia absorption liquid of each stage of branch, and the qualified ammonia water with the given concentration is continuously transferred out by adjusting the flow of the ammonia absorption liquid of each stage of branch. The temperature of the continuously transferred qualified ammonia water is controlled by adjusting the flow of the external cold water in the controllable external cold water flow cold discharge device 7.
Examples 1 to 1
As shown in FIG. 2, the ammonia concentration was adjusted to 0.595kg/m3According to 850.9m3The flow rate of the ammonia is introduced into the primary ammonia absorption monomer 1, and a primary process water pump 15 and a secondary process are simultaneously startedA water pump 16 and a three-stage process water pump 17. The third-stage process water pump 17 pumps clean water in the external process circulating water tank 13 into the third-stage ammonia absorption monomer 3; the process mixed gas in the first-stage ammonia absorption monomer 1 enters the third-stage ammonia absorption monomer 3, and ammonia absorption liquid formed after absorption by clear water respectively flows back to the second-stage ammonia absorption circulating tank 11 and the third-stage ammonia absorption circulating tank 12; then, the ammonia absorption liquid reflux liquid in the secondary ammonia absorption circulating tank 11 is used as a secondary absorption liquid, the secondary absorption liquid is pumped into the secondary ammonia absorption monomer 2 by a secondary process water pump 16 to absorb ammonia, and the ammonia absorption liquid formed after ammonia absorption further reflows into the primary ammonia absorption circulating tank 11 and the secondary ammonia absorption circulating tank 12; the ammonia absorption reflux liquid in the primary ammonia absorption circulating tank 11 is used as a primary absorption liquid and is pumped into the primary ammonia absorption monomer 1 by the primary process water pump 15 to absorb ammonia, and the ammonia absorption liquid formed after ammonia absorption respectively flows back into the primary ammonia absorption circulating tank 10 and the ammonia storage tank 9. By continuously adjusting and controlling the valves of the reflux amount of the ammonia absorption liquid in the branch pipes of the reflux pipelines and combining the detection observation of the first flowmeter 8 and the second flowmeter 14, the absorption liquid in the first-stage ammonia absorption circulating tank 10 is the high-concentration ammonia absorption liquid (the concentration value is 105.4tt), the absorption liquid in the second-stage ammonia absorption circulating tank 11 is the medium-concentration ammonia absorption liquid (the concentration value is 54.6tt), the absorption liquid in the third-stage ammonia absorption circulating tank 12 is the low-concentration ammonia absorption liquid (the concentration value is 23.2tt), the ammonia absorption liquid entering the ammonia storage tank 9 is used as a recycled ammonia water product, the concentration of the ammonia water product is the highest, and the concentration of the ammonia water product reaches the concentration value (the concentration value is 120tt) required by a qualified ammonia water recovery liquid. The statistics of the detection results of the ammonia absorption conditions in the ammonia absorption cycle sections at all stages are shown in the following table 1:
TABLE 1
Examples 1 to 2
The procedure was carried out as described in Experimental example 1-1, except that: the concentration of the ammonia is 0.578kg/m3According to 867.2m3The flow of the ammonia/h is introduced into the primary ammonia absorption monomer 1, and the reflux amount of the ammonia absorption liquid in each reflux pipeline branch is controlled by continuously adjusting a valveFinally, by combining the detection observation of the first flow meter 8 and the second flow meter 14, the absorption liquid in the first-stage ammonia absorption cycle tank 10 is a high-concentration ammonia absorption liquid (concentration value: 108.5tt), the absorption liquid in the second-stage ammonia absorption cycle tank 11 is a medium-concentration ammonia absorption liquid (concentration value: 57.4tt), the absorption liquid in the third-stage ammonia absorption cycle tank 12 is a low-concentration ammonia absorption liquid (concentration value: 24.1tt), and the statistics of the detection results of the ammonia absorption conditions in the ammonia absorption cycle sections of the above stages are shown in the following table 2:
TABLE 2
Examples 1 to 3
The procedure was followed as described in example 1-1, except that: the ammonia concentration is 0.604kg/m3According to 821.6m3And the flow rate per hour is introduced into the primary ammonia absorption monomer 1, the valve for controlling the reflux amount of the ammonia absorption liquid in each reflux pipeline branch is continuously adjusted, and the detection and observation of the first flowmeter 8 and the second flowmeter 14 are combined, so that the absorption liquid in the primary ammonia absorption circulation tank 10 is the high-concentration ammonia absorption liquid (the concentration value is 102.1tt), the absorption liquid in the secondary ammonia absorption circulation tank 11 is the medium-concentration ammonia absorption liquid (the concentration value is 53.8tt), and the absorption liquid in the tertiary ammonia absorption circulation tank 12 is the low-concentration ammonia absorption liquid (the concentration value is 22.8 tt). The statistics of the detection results of the ammonia absorption conditions in the ammonia absorption cycle sections of the above stages are shown in the following table 3:
TABLE 3
Examples 1 to 4
The procedure was followed as described in example 1-1, except that: the ammonia concentration is 0.604kg/m3According to 821.6m3The flow of the ammonia/h is introduced into the primary ammonia absorption monomer 1, and the reflux amount of the ammonia absorption liquid in each reflux pipeline branch is controlled by continuously adjusting a valve, and is combined with a first flowmeter 8The second flow meter 14 was used for detection and observation, and finally the absorption liquid in the first-stage ammonia absorption cycle tank 10 was a high-concentration ammonia absorption liquid (concentration value: 104.9tt), the absorption liquid in the second-stage ammonia absorption cycle tank 11 was a medium-concentration ammonia absorption liquid (concentration value: 56.5tt), and the absorption liquid in the third-stage ammonia absorption cycle tank 12 was a low-concentration ammonia absorption liquid (concentration value: 22.3 tt). The statistics of the detection results of the ammonia absorption conditions in the ammonia absorption cycle sections of the above stages are shown in the following table 4:
TABLE 4
The specific test results of the above embodiments show that the multistage reverse circulation ammonia absorption process of the present invention can effectively absorb ammonia gas in ammonia-containing mixed gas (process mixed gas), the ammonia gas absorption rate in each stage of circulation section is above 79%, the maximum absorption rate can reach 99.12%, and the ammonia gas concentration in gas discharged from the three-stage ammonia absorption monomer after circulation absorption is less than 0.00075. The absorption effect on ammonia gas is greatly improved, the ammonia gas can almost reach a complete absorption state, the ammonia gas leakage phenomenon does not occur in the whole absorption operation process, and the process effect is excellent.
Finally, it should be particularly noted that the above description is only given by taking the case where the ammonia absorption cycle section in the ammonia gas absorption method in the ammonia distillation process according to the present invention is a 3-stage ammonia absorption cycle as an example. One skilled in the art can easily understand that the efficiency of the multi-stage ammonia absorption process is further improved or the equipment and flow of the multi-stage ammonia absorption process are simplified by increasing or decreasing the number of stages of the multi-stage ammonia absorption cycle. More multiple ammonia absorption cycles are usually provided to improve the precision of ammonia absorption cycle control, and the complexity of the corresponding system is increased. Reducing the number of stages of the ammonia absorption cycle simplifies the equipment and the process, and if only a two-stage ammonia absorption process is adopted, the equipment only comprises two sets of cycles, the ammonia absorption efficiency can be reduced, and the pressure of the final ammonia absorption cycle is increased. The number N of ammonia absorption cycle process sections in the ammonia gas absorption method of the present invention is preferably 2 or more, including but not limited to N being 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, etc., and is a specific implementation technical solution for simply increasing or decreasing the number of ammonia absorption sections in the ammonia gas absorption method of the present invention. It is therefore preferred to use 3, 4, 5 stages of ammonia absorption cycles, preferably 3 stages of ammonia absorption cycles.
Claims (3)
1. The multistage reverse circulation ammonia absorption process is characterized by comprising N stages of ammonia absorption circulation which is carried out simultaneously, and specifically comprises the following steps:
(1) primary ammonia absorption: pumping the primary ammonia absorption liquid in the primary ammonia circulation tank into a primary ammonia absorber through a water pump, carrying out gas-liquid mixing ammonia absorption on the primary ammonia absorber and the ammonia absorption mixed gas to be absorbed introduced into the primary ammonia absorber from the outside, carrying out heat exchange treatment on ammonia water after ammonia absorption through a primary heat exchanger, and refluxing a part of ammonia water into the primary ammonia circulation tank to continuously absorb ammonia in a circulating manner;
the other part of ammonia absorption liquid with ammonia concentration reaching the specified value range is taken as a product of the ammonia absorption process and flows back to the ammonia water storage tank so as to be transferred and output;
(2) secondary ammonia absorption: pumping the secondary ammonia absorption liquid in the secondary ammonia circulation tank into a secondary ammonia absorber through a water pump, further carrying out gas-liquid mixing ammonia absorption with the ammonia-containing mixed gas which is not completely absorbed in the primary ammonia absorber, carrying out heat exchange treatment on ammonia water after ammonia absorption through a secondary heat exchanger, and refluxing a part of ammonia water to the secondary ammonia circulation tank for continuous ammonia absorption in a circulating manner;
the other part of the ammonia liquid flows back to the primary ammonia circulating tank to be used as a supplementary liquid of the primary ammonia absorption liquid;
(3) three-stage ammonia absorption: pumping the tertiary ammonia absorption liquid in the tertiary ammonia circulation tank into a tertiary ammonia absorber through a water pump, carrying out further gas-liquid mixing ammonia absorption with the ammonia-containing mixed gas which is not completely absorbed in the secondary ammonia absorber, and refluxing a part of ammonia water after ammonia absorption into the tertiary ammonia circulation tank to continuously circularly absorb ammonia after heat exchange treatment;
the other part of the ammonia flows back into a secondary ammonia circulating tank to be used as a supplementary liquid of secondary ammonia absorption liquid;
.........
(4) n-stage ammonia absorption: pumping N-grade ammonia absorption liquid in the N-grade ammonia circulation tank into the N-grade ammonia absorber through a water pump, further carrying out gas-liquid mixing ammonia absorption with ammonia-containing mixed gas which is not completely absorbed in the N-1-grade ammonia absorber, and refluxing a part of ammonia water after ammonia absorption into the N-grade ammonia circulation tank to continuously circularly absorb ammonia after heat exchange treatment;
the other part of the ammonia flows back into the N-1-level ammonia circulating tank to be used as a supplementary liquid of the N-1-level ammonia absorbing liquid;
the absorption liquid in the N-stage circulation tank is directly supplemented by external ammonia absorption liquid;
the ammonia concentration in each level of ammonia absorption liquid is gradually decreased from one level to N levels, wherein the concentration of the ammonia absorption liquid at the first level is the highest, and the concentration of the ammonia absorption liquid at the N level is the lowest;
the flow detection device is arranged at the input position of the external ammonia absorption liquid to detect the flow of the external ammonia absorption liquid input into the ammonia absorption circulating system;
the flow detection device is arranged at the inlet of the ammonia storage tank, so that the flow of the transferred and output ammonia absorption liquid product is detected;
the flow of the ammonia absorption liquid in the ammonia circulation tank and the ammonia storage tank communicated with the ammonia absorber at each stage is controlled by a valve, so that the concentration of the ammonia absorption liquid in the ammonia circulation tank at each stage and the ammonia concentration of the ammonia absorption liquid entering the ammonia storage tank are effectively controlled.
2. The multistage reverse circulation ammonia absorption process as claimed in claim 1, wherein the number of N in the N absorption cycle is 3.
3. A multistage reverse circulation ammonia absorption process according to any one of claims 1 to 2, wherein: and a heat exchanger capable of controlling the flow of an external cooling substance is connected between the primary ammonia absorber and the ammonia storage tank, so that the temperature of ammonia water flowing back to the ammonia storage tank is controlled.
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