CN111992026B - Denitration double-reactor arrangement method and system for realizing online switching - Google Patents

Denitration double-reactor arrangement method and system for realizing online switching Download PDF

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CN111992026B
CN111992026B CN202010700446.0A CN202010700446A CN111992026B CN 111992026 B CN111992026 B CN 111992026B CN 202010700446 A CN202010700446 A CN 202010700446A CN 111992026 B CN111992026 B CN 111992026B
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reactor
insulating layer
heat
main
main reactor
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CN111992026A (en
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金舒杰
陈介平
王汉平
陆云海
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ZHANGJIAGANG JINMING MACHINERY CO Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/90—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0241—Other waste gases from glass manufacture plants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases

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  • Environmental & Geological Engineering (AREA)
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Abstract

The invention disclosesA denitration double-reactor arrangement method and a denitration double-reactor arrangement system for realizing online switching are provided, and the method comprises the following steps: configuring a main reactor and a standby reactor; an insulating layer a is arranged on the main reactor; input the initial temperature t of the main reactor medium1Terminal temperature t of the main reactor medium2And the temperature t of the air surrounding the primary reactork(ii) a Establishing a calculation model of the heat temperature drop-the outer diameter of the heat preservation layer, and calculating the outer diameter d of the heat preservation layer a1(ii) a Calculating the thickness delta of the heat preservation layer a; an insulating layer b with the same thickness as the insulating layer a is arranged on the standby reactor; a heat preservation space is arranged between the main reactor and the standby reactor. The main reactor and the standby reactor form a double-reactor system, online switching can be realized, non-stop maintenance is realized, the problem of excessive discharge caused by stop maintenance is effectively solved, the whole switching process is quicker, the switching time is greatly reduced, and the excessive discharge time is reduced to the minimum.

Description

Denitration double-reactor arrangement method and system for realizing online switching
Technical Field
The invention relates to the technical field of glass production, in particular to a denitration double-reactor arrangement method and a denitration double-reactor arrangement system for realizing online switching.
Background
The glass trade generally uses SCR deNOx systems, and current system need be shut down when overhauing, and the shut down of short time is overhauld and can be caused the problem that the emission exceeds standard, can not adapt to the environmental protection policy that becomes stricter day by day, consequently does not shut down the maintenance and will become must trend, and this wherein, the maintenance of not shutting down of SCR deNOx reactor will be the key that influences whole deNOx systems, has very big help to reducing the problem of shutting down to exceed standard. At present, no denitration system capable of realizing online maintenance exists in the glass production industry.
Disclosure of Invention
One object of the invention is to provide a denitration double-reactor arrangement method for realizing online switching, which comprises the following steps:
s1, configuring a main reactor and a standby reactor;
s2, arranging a heat-insulating layer a on the primary reactor;
s3, inputting the initial end temperature t of the main reactor medium1Terminal temperature t of the primary reactor medium2And the temperature t of the air surrounding the primary reactork；
S4, establishing a heat temperature drop-heat preservation layer outer diameter calculation model, and calculating the outer diameter d of the heat preservation layer a1；
S5, calculating the thickness delta of the heat preservation layer a;
s6, arranging an insulating layer b with the same thickness as the insulating layer a on the spare reactor;
and S7, arranging the main reactor and the standby reactor adjacently, and arranging a heat preservation space between the main reactor and the standby reactor.
By adopting the technical scheme, step S4 is (t)1-tk)/(t2-tk) When < 2, the outer diameter d of the insulating layer a is calculated by using the formula (1)1：
ln(d1/dw)＝2×3.14×λ1×[(tp-tk)×L×K1/[G×C×(t1-t2)－αh·1]In the formula (1),
in the formula (d)wIs an inner diameter of a heat-insulating layer a, lambda1Is the thermal conductivity coefficient W/m DEG C of the thermal insulation material, tpThe average temperature of the heat-insulating layer a is higher than the average temperature of the heat-insulating layer a, and L is the length m and K of the main reactor body1The local heat preservation coefficient of the installation support of the primary reactor, G is the medium flow rate in the primary reactor kg/h, C is the average specific heat kj/(kg DEG C) of the medium, and alphah·1The heat release coefficient W/(m) from the insulating layer a to the surrounding air2·k)。
By adopting the technical scheme, step S4 is (t)1-tk)/(t2-tk) When the temperature is more than or equal to 2, calculating the outer diameter d of the heat-insulating layer a by using the formula (2)1：
ln(d1/dw)＝2×3.14×λ1×[(t2-tk)×L×K1/[G×C×(t1-tk)－αh·1]In the formula (2),
in the formula (d)wIs an inner diameter of a heat-insulating layer a, lambda1The thermal conductivity coefficient W/m.DEG C of the thermal insulation material is the main useLength m, K of reactor body1The local heat preservation coefficient of the installation support of the main reactor, G is the medium flow rate kg/h in the main reactor body, C is the average specific heat kj/(kg DEG C) of the medium, and alpha ish·1The heat release coefficient W/(m) from the insulating layer a to the surrounding air2·k)。
By adopting the technical scheme, the formula for calculating the thickness delta of the heat-insulating layer a in S5 is as follows:
δ＝(d1-dw) Formula/2 (3)
In the formula (d)1Is the outer diameter of the heat-insulating layer a, dwThe inner diameter of the heat insulation layer a.
By adopting the technical scheme, the heat insulation distance is 1.2-1.8 times of the thickness of the heat insulation layer a.
The invention also aims to provide a denitration double-reactor system for realizing online switching, which comprises a main reactor and a standby reactor, wherein the main reactor and the standby reactor are arranged by using the denitration double-reactor arrangement method for realizing online switching.
By adopting the technical scheme, the main reactor comprises a main reactor inlet baffle and a main reactor outlet baffle, and the main reactor inlet baffle and the main reactor outlet baffle are respectively arranged at the inlet position and the outlet position of the main reactor.
Technical scheme more than adopting, spare reactor includes spare reactor entry baffle and spare reactor exit baffle, spare reactor entry baffle and spare reactor exit baffle locate the entry position and the exit position of spare reactor respectively.
By adopting the technical scheme, the system comprises a flue gas source, wherein the inlet baffle of the main reactor and the inlet baffle of the standby reactor are respectively and jointly connected to the flue gas source through the input flue, and the outlet baffle of the main reactor and the outlet baffle of the standby reactor are jointly connected to the output flue.
By adopting the technical scheme, the system also comprises a main reactor blower and a standby reactor blower, wherein the main reactor blower and the standby reactor blower are respectively connected to the main reactor and the standby reactor.
The invention has the beneficial effects that: the invention comprises a main reactor and a standby reactor, wherein the main reactor and the standby reactor form a double-reactor system, so that online switching can be realized, non-shutdown maintenance is realized, the problem of excessive discharge caused by shutdown maintenance is effectively reduced, a fixed heat transfer effect can be ensured by calculating the thickness of a heat insulation layer of the main reactor and arranging a heat insulation space between the main reactor and the standby reactor, a certain temperature rise effect is achieved on the standby reactor, the temperature rise time of a catalyst in the standby reactor is greatly reduced, the whole switching process can be quicker, the switching time is greatly reduced, and the excessive discharge time is reduced to the minimum.
Drawings
FIG. 1 is a flow chart of a denitration double-reactor arrangement method for realizing online switching according to an embodiment of the invention.
FIG. 2 is a schematic layout diagram of a denitration double-reactor layout method for realizing online switching according to an embodiment of the present invention.
FIG. 3 is a block diagram of a denitration double-reactor system for realizing online switching according to an embodiment of the present invention.
The reference numbers are as follows: 1. a primary reactor; 11. an inlet baffle of the main reactor; 12. an outlet baffle of the main reactor; 13. a primary reactor blower; 14. an insulating layer a; 2. a standby reactor; 21. a spare reactor inlet baffle; 22. a standby reactor outlet baffle; 23. a standby reactor blower; 24. a heat-insulating layer b; 3. a source of flue gas; 4. inputting a flue; 5. an output flue; 6. an air source; 7. keeping the temperature for a certain distance;
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
Examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are illustrative and intended to be illustrative of the invention and are not to be construed as limiting the invention.
Fig. 1 and fig. 2 show a denitration double-reactor arrangement method for realizing online switching according to an embodiment of the present invention, where the method 1 starts with step S1, and in step S1, a primary reactor 1 and a backup reactor 2 are configured; thereafter, step S2 is executed
In step S2, an insulating layer a14 is provided on the primary reactor; thereafter, step S3 is executed
In step S3, the start temperature t of the primary reactor 1 medium is input1Terminal temperature t of the main reactor 2 medium2And the temperature t of the air surrounding the primary reactor 1k(ii) a Thereafter, step S4 is executed
In step S4, a calculation model of the heat temperature drop-insulating layer outer diameter is created, and the outer diameter d of the insulating layer a14 is calculated1(ii) a Thereafter, step S5 is executed
In step S5, the thickness δ of the heat-insulating layer a14 is calculated using formula (3),
δ＝(d1-dw) Formula/2 (3)
In the formula, d1Is an insulating layer a14 with an external diameter dwThe inner diameter of the heat-insulating layer a 14; then step S6 is executed;
in step S6, an insulating layer b24 having the same thickness as the insulating layer a14 is provided on the spare reactor 2; thereafter, step S7 is executed
In step S7, the primary reactor 1 and the backup reactor 2 are arranged adjacent to each other, and a heat-insulating space is provided between the primary reactor 1 and the backup reactor 2.
In the case of the present embodiment, in step S4,
when (t)1-tk)/(t2-tk) If < 2, the step S4-1 is executed to calculate the outer diameter d of the heat-insulating layer a141：
In step S4-1, it is calculated using equation (1):
ln(d1/dw)＝2×3.14×λ1×[(tp-tk)×L×K1/[G×C×(t1-t2)－αh·1]in the formula (1),
in the formula (d)wIs an insulating layer a14 with an inner diameter of lambda1Is the thermal conductivity coefficient W/m DEG C of the thermal insulation material, tpThe average temperature of the heat-insulating layer a14 ℃, L is the length m and K of the main reactor 11The local heat preservation coefficient of the installation support of the main reactor 1, G is the medium flow rate kg/h in the main reactor 1, C is the average specific heat kj/(kg DEG C.) of the medium, and alphah·1The heat release coefficient W/(m) from the heat-insulating layer a14 to the surrounding air2·k)；
When (t)1-tk)/(t2-tk) When the temperature is more than or equal to 2, the step S4-2 is executed to calculate the outer diameter d1 of the insulating layer a 14:
in step S3-2, it is calculated using equation (2):
ln(d1/dw)＝2×3.14×λ1×[(t2-tk)×L×K1/[G×C×(t1-tk)－αh·1]in the formula (2),
in the formula (d)wIs an insulating layer a14 with an inner diameter of lambda1The thermal conductivity coefficient W/m.DEG C of the thermal insulation material is L which is the length m and K of the main reactor 1 body1The local heat preservation coefficient of the installation support of the main reactor 1, G is the medium flow rate kg/h in the main reactor 1 body, C is the average specific heat kj/(kg DEG C.) of the medium, and alphah·1The heat release coefficient W/(m) from the heat insulation layer a14 to the ambient air2·k)。
Based on the situation of the embodiment, the heat preservation space 7 is 1.2-1.8 times the thickness of the heat preservation layer a14, and the proper heat preservation space 7 can ensure a fixed heat transfer effect, so that when the primary reactor 1 works, a certain temperature rise effect can be achieved on the standby reactor 2.
FIG. 3 shows a denitration double-reactor system for realizing online switching according to an embodiment of the present invention, which includes a main reactor 1 and a spare reactor 2, the main reactor 1 and the spare reactor 2 are adjacently arranged to form the double-reactor system, a thermal insulation layer a14 is arranged on the main reactor 1, the thickness of the thermal insulation layer a14 is calculated by the above method, so as to ensure that the main reactor 1 is in a reasonable temperature drop interval, a thermal insulation layer b24 with the same thickness as the thermal insulation layer a14 is arranged on the spare reactor 2, and a thermal insulation space 7 is arranged between the main reactor 1 and the spare reactor 2, on the premise of ensuring that the temperature of SCR denitration is in a certain range, a certain temperature rise can be provided for the spare reactor 2, the temperature rise time of a catalyst inside the spare reactor 2 is greatly reduced, the whole switching process can be more rapid, and the switching time is greatly reduced, minimizing the time to over-standard emissions.
The system also comprises a flue gas source 3 and an air source 6, wherein the main reactor 1 and the standby reactor 2 are jointly connected with the flue gas source 3 and the air source 6, so that the online switching between the main reactor 1 and the standby reactor 2 can be realized, for example, when the main reactor 1 needs to be overhauled, the main reactor 1 is closed, and the standby reactor 2 is opened, so that flue gas is rapidly switched from the main reactor 1 to the standby reactor 2.
Based on the situation of the embodiment, the primary reactor 1 includes a primary reactor inlet baffle 11 and a primary reactor outlet baffle 12, and the primary reactor inlet baffle 11 and the primary reactor outlet baffle 12 are respectively arranged at the inlet position and the outlet position of the primary reactor 1;
the spare reactor 2 comprises a spare reactor inlet baffle 21 and a spare reactor outlet baffle 22, and the spare reactor inlet baffle 21 and the spare reactor outlet baffle 22 are respectively arranged at the inlet position and the outlet position of the spare reactor 2;
in summary, the primary reactor inlet baffle 11 and the backup reactor inlet baffle 12 are connected to the flue gas source 3 through the input flue 4, and the primary reactor outlet baffle 12 and the backup reactor outlet baffle 22 are connected to the output flue 5.
Based on the situation of the embodiment, the system further comprises a main reactor blower 13 and a standby reactor blower 23, wherein the main reactor blower 13 and the standby reactor blower 23 are respectively connected to the main reactor 1 and the standby reactor 2, and the main reactor blower 13 and the standby reactor blower 23 are respectively connected to the air source 6 through pipelines; of course, other arrangements of the system such as a fairing, a static mixer, and a purge system are also contemplated.
When the system is in actual use and needs to be switched, the auxiliary equipment related to the main reactor 1 is closed in advance, after the switching is confirmed not to be influenced, the inlet baffle plate 11 of the main reactor is closed, and the inlet baffle plate 21 of the standby reactor is opened at the same time, so that flue gas is rapidly switched from the main reactor 1 to the standby reactor 2, and when the temperature of the flue gas is raised, the flue gas conditions meet the operation requirements, the auxiliary equipment related to the standby reactor 2 is opened.
The invention has the beneficial effects that: the invention comprises a main reactor and a standby reactor, wherein the main reactor and the standby reactor form a double-reactor system, online switching can be realized, non-shutdown maintenance is realized, and the problem of discharge standard exceeding caused by shutdown maintenance is effectively reduced.
The above embodiments are merely preferred embodiments for fully illustrating the present invention, and the scope of the present invention is not limited thereto. The equivalent substitution or change made by the technical personnel in the technical field on the basis of the invention is all within the protection scope of the invention. The protection scope of the invention is subject to the claims.

Claims (8)

1. A denitration double-reactor arrangement method for realizing online switching is characterized by comprising the following steps:
s1, configuring a main reactor and a standby reactor;
s2, arranging a heat-insulating layer a on the primary reactor;
s3, inputting the initial end temperature t of the main reactor medium1Terminal temperature t of the main reactor medium2And the temperature t of the air surrounding the primary reactork；
S4, establishing a heat temperature drop-heat preservation layer outer diameter calculation model, and calculating the outer diameter d of the heat preservation layer a1The method comprises the following steps:
when (t)1-tk)/(t2-tk) When the temperature is less than 2, the external diameter d of the insulating layer a is calculated by using the formula (1)1：
ln(d1/dw)＝2×3.14×λ1×[(tp-tk)×L×K1/[G×C×(t1-t2)－αh·1]In the formula (1),
in the formula (d)wIs an inner diameter of a heat-insulating layer a, lambda1The thermal conductivity coefficient W/m DEG C of the thermal insulation material is tpThe average temperature of the heat-insulating layer a is higher than the average temperature of the heat-insulating layer a, and L is the length m and K of the main reactor body1The local heat preservation coefficient of the installation support of the primary reactor, G is the medium flow rate in the primary reactor kg/h, C is the average specific heat kj/(kg DEG C) of the medium, and alphah·1The heat release coefficient W/(m) from the insulating layer a to the surrounding air2·k)；
When (t)1-tk)/(t2-tk) When the temperature is more than or equal to 2, calculating the outer diameter d of the heat-insulating layer a by using the formula (2)1：
ln(d1/dw)＝2×3.14×λ1×[(t2-tk)×L×K1/[G×C×(t1-tk)－αh·1]In the formula (2),
in the formula (d)wIs an inner diameter of a heat-insulating layer a, lambda1The thermal conductivity coefficient W/m.DEG C of the thermal insulation material, L is the length m, K of the main reactor body1The local heat preservation coefficient of the installation support of the main reactor, G is the medium flow rate kg/h in the main reactor body, C is the average specific heat kj/(kg DEG C.) of the medium, and alphah·1The heat release coefficient W/(m) from the insulating layer a to the surrounding air2·k)；
S5, calculating the thickness delta of the heat preservation layer a;
s6, arranging an insulating layer b with the same thickness as the insulating layer a on the spare reactor;
and S7, arranging the main reactor and the standby reactor adjacently, and arranging a heat preservation space between the main reactor and the standby reactor.
2. The denitration double-reactor arrangement method for realizing online switching according to claim 1, characterized in that: the formula for calculating the thickness δ of the insulating layer a in S5 is as follows:
δ＝(d1-dw) Formula/2 (3)
In the formula (d)1Is outside the heat-insulating layer aDiameter, dwThe inner diameter of the heat insulation layer a.
3. The denitration double-reactor arrangement method for realizing online switching according to claim 1, characterized in that: the heat preservation interval is 1.2-1.8 times of the thickness of the heat preservation layer a.
4. The utility model provides a realize denitration double reactor system of online switching which characterized in that: the system comprises a main reactor and a standby reactor, wherein the main reactor and the standby reactor are arranged by using the denitration double-reactor arrangement method for realizing online switching according to any one of claims 1 to 3.
5. The denitration double-reactor system for realizing online switching as set forth in claim 4, wherein: the main reactor comprises a main reactor inlet baffle and a main reactor outlet baffle, and the main reactor inlet baffle and the main reactor outlet baffle are respectively arranged at the inlet position and the outlet position of the main reactor.
6. The denitration double-reactor system for realizing online switching according to claim 4, wherein: spare reactor includes spare reactor entry baffle and spare reactor export baffle, spare reactor entry baffle and spare reactor export baffle are located spare reactor's entry position and exit position respectively.
7. The denitration double-reactor system for realizing online switching according to claim 4, wherein: the system comprises a flue gas source, wherein a main reactor inlet baffle and a standby reactor inlet baffle are respectively and jointly connected into the flue gas source through an input flue, and a main reactor outlet baffle and a standby reactor outlet baffle are jointly connected into an output flue.
8. The denitration double-reactor system for realizing online switching according to claim 4, wherein: the system also comprises a main reactor blower and a standby reactor blower, wherein the main reactor blower and the standby reactor blower are respectively connected into the main reactor and the standby reactor.
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