CN207581358U - One kind contains SO3Gas relieving haperacidity energy recycle device - Google Patents
One kind contains SO3Gas relieving haperacidity energy recycle device Download PDFInfo
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- CN207581358U CN207581358U CN201820467861.4U CN201820467861U CN207581358U CN 207581358 U CN207581358 U CN 207581358U CN 201820467861 U CN201820467861 U CN 201820467861U CN 207581358 U CN207581358 U CN 207581358U
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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
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Abstract
The utility model discloses one kind to contain SO3Gas relieving haperacidity energy recycle device, belongs to novel and is related to chemical field.The device directly generates low-pressure steam using the outer heat for sulfuric acid, then process gas pipeline before feeding reaction tower, it substitutes section mixer and adds water, reduce the live load of mixer, reduce recycle acid flow, reduce the power consumption of circulating pump, more importantly in the case where in addition not consuming energy, the heat of low steam (0.15 ± 0.05MPa (g)) switchs to the heat for high temperature concentrated acid (190 ± 30 DEG C), and passes through the low-pressure steam that more higher pressures (0.8 ± 0.4MPa (g)) is generated in evaporator.Can real low-heat recovery system often produce 1 ton of sulfuric acid can be with 0.55 ± 0.1 ton of low-pressure steam of by-product.
Description
Technical field
The utility model is related to chemical fields, and in particular to one kind contains SO3Gas relieving haperacidity energy recycle device.
Background technology
Gas washing in SA production industry at present, particularly in ore deposit or metallurgical off-gas acid-making industry, many device SO3By H2O absorbs production
The energy of sulfuric acid reaction is usually taken to by recirculated water in air, is wholly or largely wasted.This technological process does not have not only
It brings benefits, and needs to consume a large amount of recirculated waters.There are partial devices to be provided with low temperature heat reclamation device in dry absorption section,
Technical process is：Containing SO3Process gas enter high temperature absorption tower, absorbed by spray acid in tower, release heat, acid temperature
Raising, high temperature concentrated acid send pressurization to be sent into evaporator and generate low-pressure steam, enter mixer after sour temperature drop is low by high temperature circulation pumping
Water is added to reduce sour dense, be then re-fed into high temperature absorption tower cyclic absorption SO3；Device production acid is from the cycle acid tube of evaporator outlet
It picks out, it is outer after feed-water heater and the cooling of desalination water heater to supply, it returns metallurgical off-gas acid-making due to ore deposit and does and inhale low temperature recuperation of heat
System is higher for ratio of the sulfuric acid in recycle acid outside, outer for usually 130 DEG C~160 DEG C of acid temperature, still has partial heat to fail
Effectively recycling, this part, which sends sulfuric acid outside, can add in the relatively low processing medium of other temperature, it is impossible to generate low-pressure steam, energy regenerating
Quality is low, and use scope is limited.In this kind of low temperature heat reclamation device, the direct steam generating capacity of low-pressure steam generally often produces 1
0.25~0.40t of ton sulphuric acid production low-pressure steam or so, still has partial heat and underuses.
Utility model content
The utility model is to provide SO in view of the shortcomings of the prior art3Gas relieving haperacidity energy recycle device and method.
The purpose of this utility model can be achieved through the following technical solutions：
One kind contains SO3Gas relieving haperacidity energy recycle device, the device include reaction tower, evaporator and evaporation oxygen-eliminating device, institute
The bottom for the reaction tower stated is connected by circulating pump with evaporator, an output terminal of the evaporator by mixer with it is anti-
The top of tower is answered to be connected, another output terminal of the evaporator successively with evaporator feedwater heater, evaporation oxygen-eliminating device and
Desalination water preheater is connected, containing SO3The output channel of process gas be connected with the bottom of reaction tower.
In some specific technical solutions：The output terminal of desalted water is by desalination water preheater with evaporating oxygen-eliminating device phase
Even, an output terminal of described evaporation oxygen-eliminating device bottom by low pressure feed water pump successively with evaporator feedwater heater and evaporation
The input terminal of device is connected, another output terminal is pumped by low pressure feed water to be connected with mixer.
In some specific technical solutions：Output terminal at the top of the evaporation oxygen-eliminating device is with containing SO3Process gas
Output channel be connected.
A kind of method that energy regenerating is realized using above-mentioned device, it is characterised in that：This method includes the following steps：
(1) containing SO3Process gas before reaction tower is entered, the low-pressure steam that is first generated with evaporation oxygen-eliminating device by 60 ±
40:1 mass ratio mixing, containing SO3Process gas in part or all of SO3Generation H is reacted with low-pressure steam2SO4, it is described
Process gas temperature raising after enter reaction tower after with top spray under recycle acid the reaction was continued, react the high-temperature sulfuric acid of generation
Evaporator is sent into after circulating pump pressurizes generate low-pressure steam, the process gas reaction lower work of rear molding pneumatic transmission after tower bottom converges
Sequence processing；
(2) 85 ± 10% high-temperature sulfuric acid, which goes out, enters mixer after evaporator, with low pressure feed water reduce acid it is dense after enter back into
SO in reaction tower cyclic absorption process gas3, remaining high-temperature sulfuric acid is picked out from evaporator outlet recycle acid pipeline, advanced
Enter the heating of evaporator feedwater heater and be sent into low pressure feed water, enter back into evaporation oxygen-eliminating device thermal de-aeration and generate low-pressure steam, most
Enter desalted water preheater afterwards, preheat room temperature desalted water, sulfuric acid send downstream process to handle after cooling；
(3) the extraneous room temperature desalted water being sent into, is first heated in desalination water preheater, is re-fed into evaporation oxygen-eliminating device later and is added
Heat generates low-pressure steam simultaneously in thermal de-aeration, and low-pressure steam send reaction tower import and the SO in process gas3Reaction, evaporation
For deaerated water in oxygen-eliminating device after low pressure feed water pump pressurization, 25 ± 15% low pressure feed water send mixer to reduce cycle acid concentration,
Remaining low pressure feed water send evaporator feedwater heater, and evaporator is re-fed into after heating and generates low-pressure steam.
In some specific technical solutions：The pressure for the low-pressure steam that evaporation oxygen-eliminating device (6) generates is in step (1)
0.2 ± 0.1MPa, the temperature of circulating pump (2) outlet high-temperature sulfuric acid is 190 ± 30 DEG C, the low-pressure steam pressure that evaporator (3) generates
Power is 0.8 ± 0.4MPa.
This is gauge pressure using the pressure described in careful technical solution.
The beneficial effects of the utility model：
Contain SO using of the present invention3Gas relieving haperacidity energy recycle device is directly generated using the outer heat for sulfuric acid
Low-pressure steam is then sent into process gas pipeline before reaction tower, substitutes section mixer and adds water, the work for reducing mixer is born
Lotus reduces recycle acid flow, reduces the power consumption of circulating pump, it is often more important that in the case where in addition not consuming energy,
The heat of low steam (0.15 ± 0.05MPa (g)) switchs to the heat for high temperature concentrated acid (190 ± 30 DEG C), and passes through in evaporator
Generate the low-pressure steam of more higher pressures (0.8 ± 0.4MPa (g)).Can real low-heat recovery system often produce 1 ton of sulfuric acid can
With 0.55 ± 0.1 ton of low-pressure steam of by-product.
Description of the drawings
Fig. 1 contains SO to be a kind of3The schematic diagram of gas relieving haperacidity energy recycle device.
Wherein：1 is reaction tower, and 2 be circulating pump, and 3 be evaporator, and 4 be mixer, and 5 be evaporator feedwater heater, and 6 are
Oxygen-eliminating device is evaporated, 7 be desalination water preheater, and 8 pump for low pressure feed water.
Specific embodiment
The utility model is described further, but the scope of protection of the utility model is not limited to reference to embodiment
This：
With reference to embodiment, the present invention will be further described, and but the scope of the present invention is not limited thereto：Technical side
Case：
Such as Fig. 1, one kind contains SO3Gas relieving haperacidity energy recycle device, the device include reaction tower (1), evaporator (3) and steam
Oxygen-eliminating device (6) is sent out, the bottom of the reaction tower (1) is connected by circulating pump (2) with evaporator (3), the evaporator (3)
An output terminal be connected by mixer (4) with the top of reaction tower (1), another output terminal of the evaporator (3)
Pass sequentially through evaporator feedwater heater (5), evaporation oxygen-eliminating device (6) be connected with desalination water preheater (7), containing SO3Process gas
The output channel of body is connected with the bottom of reaction tower (1).
The output terminal of desalted water is connected by desalination water preheater (7) with evaporation oxygen-eliminating device (6), the evaporation oxygen-eliminating device
(6) it is defeated with evaporator feedwater heater (5) and evaporator (3) successively by low pressure feed water to pump (8) for an output terminal of bottom
Enter end to be connected, another output terminal pumps (8) by low pressure feed water and with mixer (4) is connected.
Output terminal at the top of the evaporation oxygen-eliminating device (6) is with containing SO3The output channel of process gas be connected.
It is realized using device shown in FIG. 1 containing SO3Gas relieving haperacidity energy reclaiming method, it is specific such as embodiment 1-1,1-2,1-
3。
Embodiment 1-1
Containing SO3Process gas before reaction tower (1) is entered, 0.1MPa (g) low pressure that is first generated with evaporation oxygen-eliminating device (6)
Steam presses 30:1 mass ratio mixes, part SO in process gas3Generation sulfur process gas temperature liter is reacted with low-pressure steam
Height, process gas body temperature are upgraded to 40 DEG C, and into reaction tower (1), the reaction was continued with the recycle acid under the spray of top for process gas afterwards, instead
200 DEG C of high-temperature sulfuric acid should be generated and be sent into evaporator (3) generation 0.6MPa after circulating pump (2) pressurization after tower bottom converges
(g) low-pressure steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
80% high-temperature sulfuric acid goes out evaporator (3) and enters mixer (4) afterwards, with low pressure feed water reduce acid it is dense after enter back into it is anti-
Answer the SO in tower (1) cyclic absorption process gas3, the high-temperature sulfuric acid of remainder is from evaporator (3) outlet recycle acid pipeline
It picks out, is introduced into evaporator feedwater heater (5) heating and is sent into low pressure feed water, enter back into evaporation oxygen-eliminating device (6) thermal de-aeration simultaneously
Low-pressure steam 0.1MPa is generated, finally enters desalination water preheater, preheats room temperature desalted water, it is outer to drop to 105 for sulfuric acid temperature
DEG C downstream process is sent to handle.
The room temperature desalted water that the external world is sent into first is heated to 100 DEG C in desalination water preheater (7), is re-fed into evaporation deoxygenation
Device (6), is heated to 120 DEG C, and thermal de-aeration generates 0.1MP (g) low-pressure steams simultaneously, low-pressure steam send reaction tower (1) import with
SO in process gas3Reaction evaporates the deaerated water in oxygen-eliminating device (6) after low pressure feed water pumps (8) pressurization, and 10% low pressure is given
Water send mixer (4) to reduce cycle acid concentration, remaining to send evaporator feedwater heater (5), is heated to 160 DEG C, is steamed being sent into
Send out the low-pressure steam that device generates 0.6MPa.
It is significantly reduced using the technical program compared with outside the prior art for sulfuric acid temperature, it can be achieved that sulfuric acid by-product 0.595 per ton
Ton low-pressure steam.
Embodiment 1-2
Containing SO3Process gas before reaction tower (1) is entered, it is first low with the 0.15MPa (g) of evaporation oxygen-eliminating device (6) generation
Steam is pressed to press 50:1 mass ratio mixes, part SO in process gas3Generation sulfur process gas temperature is reacted with low-pressure steam
Raising, process gas body temperature are upgraded to 55 DEG C, and into reaction tower (1), the reaction was continued with the recycle acid under the spray of top for process gas afterwards,
The high-temperature sulfuric acid that reaction generates 210 DEG C is sent into evaporator (3) generation 0.8MPa after tower bottom converges after circulating pump (2) pressurization
(g) low-pressure steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
85% high-temperature sulfuric acid goes out that evaporator (3) is most of afterwards to enter mixer (4), with low pressure feed water reduce acid it is dense after again
SO into reaction tower (1) cyclic absorption process gas3, remaining high-temperature sulfuric acid connects from evaporator outlet recycle acid pipeline
Go out, be introduced into evaporator feedwater heater (5) heating and be sent into low pressure feed water, enter back into evaporation oxygen-eliminating device (6) thermal de-aeration and produce
Raw low-pressure steam 0.15MPa, finally enters desalination water preheater, preheats room temperature desalted water, outer to drop to 115 DEG C for sulfuric acid temperature
Downstream process is sent to handle.
The room temperature desalted water that the external world is sent into first is heated to 110 DEG C in desalination water preheater (7), is re-fed into evaporation deoxygenation
Device (6) is heated to 127 DEG C, and thermal de-aeration generates 0.15MP low-pressure steams simultaneously, and low-pressure steam send reaction tower (1) import and work
SO in skill gas3Reaction evaporates the deaerated water in oxygen-eliminating device (6) after low pressure feed water pumps (8) pressurization, 20% low pressure feed water
Mixer (4) is sent to reduce cycle acid concentration, remainder dispensing evaporator feedwater heater (5) is heated to 170 DEG C, is steamed being sent into
Send out the low-pressure steam that device generates 0.8MPa.
It is significantly reduced using the technical program compared with outside the prior art for sulfuric acid temperature, it can be achieved that sulfuric acid by-product 0.584 per ton
Ton low-pressure steam.
Embodiment 1-3
Containing SO3Process gas before reaction tower (1) is entered, 0.2MPa (g) low pressure that is first generated with evaporation oxygen-eliminating device (6)
Steam presses 90:1 mass ratio mixes, part SO in process gas3Generation H is reacted with low-pressure steam2SO process gas temperature liters
Height, process gas body temperature are upgraded to 70 DEG C, and into reaction tower (1), the reaction was continued with the recycle acid under the spray of top for process gas afterwards, instead
220 DEG C of high-temperature sulfuric acid should be generated and be sent into evaporator (3) generation 1.2MPa after circulating pump (2) pressurization after tower bottom converges
(g) low-pressure steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
95% high-temperature sulfuric acid goes out evaporator (3) mixer (4) afterwards, with low pressure feed water reduce acid it is dense after enter back into reaction tower
(1) SO in cyclic absorption process gas3, remaining high-temperature sulfuric acid picks out from evaporator outlet recycle acid pipeline, is introduced into
Low pressure feed water is sent into evaporator feedwater heater (5) heating, is entered back into evaporation oxygen-eliminating device (6) thermal de-aeration and is generated low-pressure steam
0.2MPa finally enters desalination water preheater, preheats room temperature desalted water, and outer confession sulfuric acid temperature drops to 130 DEG C and send downstream process
Processing.
The room temperature desalted water that the external world is sent into first is heated to 120 DEG C in desalination water preheater (7), is re-fed into evaporation deoxygenation
Device (6), is heated to 133 DEG C, and thermal de-aeration generates 0.2MP (g) low-pressure steams simultaneously, low-pressure steam send reaction tower (1) import with
SO in process gas3Reaction evaporates the deaerated water in oxygen-eliminating device (6) after low pressure feed water pumps (8) pressurization, and 40% low pressure is given
Water send mixer (4) to reduce cycle acid concentration, and remainder dispensing evaporator feedwater heater (5) is heated to 185 DEG C, is being sent into
Evaporator generates the low-pressure steam of 1.2MPa.
It is significantly reduced using the technical program compared with outside the prior art for sulfuric acid temperature, it can be achieved that sulfuric acid by-product 0.578 per ton
Ton low-pressure steam.
Claims (3)
1. one kind contains SO3Gas relieving haperacidity energy recycle device, it is characterised in that：The device include reaction tower (1), evaporator (3) and
Oxygen-eliminating device (6) is evaporated, the bottom of the reaction tower (1) is connected by circulating pump (2) with evaporator (3), the evaporator
(3) a output terminal is connected by mixer (4) with the top of reaction tower (1), another output of the evaporator (3)
End is connected successively with evaporator feedwater heater (5), evaporation oxygen-eliminating device (6) and desalination water preheater (7), containing SO3Process gas
The output channel of body is connected with the bottom of reaction tower (1).
2. according to claim 1 contain SO3Gas relieving haperacidity energy recycle device, it is characterised in that：The output terminal of desalted water leads to
It crosses desalination water preheater (7) with evaporation oxygen-eliminating device (6) to be connected, an output terminal of described evaporation oxygen-eliminating device (6) bottom passes through
Low pressure feed water pumps the input terminal of (8) successively with evaporator feedwater heater (5) and evaporator (3) and is connected, another output terminal leads to
Low pressure feed pump (8) is crossed with mixer (4) to be connected.
3. according to claim 1 contain SO3Gas relieving haperacidity energy recycle device, it is characterised in that：The evaporation oxygen-eliminating device
(6) output terminal at the top of is with containing SO3The output channel of process gas be connected.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820467861.4U CN207581358U (en) | 2018-04-02 | 2018-04-02 | One kind contains SO3Gas relieving haperacidity energy recycle device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820467861.4U CN207581358U (en) | 2018-04-02 | 2018-04-02 | One kind contains SO3Gas relieving haperacidity energy recycle device |
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| CN207581358U true CN207581358U (en) | 2018-07-06 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108483409A (en) * | 2018-04-02 | 2018-09-04 | 南京海陆化工科技有限公司 | One kind containing SO3Gas relieving haperacidity energy recycle device and method |
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2018
- 2018-04-02 CN CN201820467861.4U patent/CN207581358U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108483409A (en) * | 2018-04-02 | 2018-09-04 | 南京海陆化工科技有限公司 | One kind containing SO3Gas relieving haperacidity energy recycle device and method |
| WO2019192173A1 (en) * | 2018-04-02 | 2019-10-10 | 南京海陆化工科技有限公司 | Acid generation energy recovery device and method for so3-containing gas |
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