CN207581359U - 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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- CN207581359U CN207581359U CN201820467862.9U CN201820467862U CN207581359U CN 207581359 U CN207581359 U CN 207581359U CN 201820467862 U CN201820467862 U CN 201820467862U CN 207581359 U CN207581359 U CN 207581359U
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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 present invention relates to chemical fields, and in particular to one kind contains SO3Gas relieving haperacidity energy recycle device and method.
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.
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, evaporator feedwater heating
Device mixer is connected with the top of reaction tower, another output terminal of evaporator adds successively with evaporation oxygen-eliminating device and evaporator feedwater
Hot device is connected with desalination water preheater, containing SO3The output channel of process gas be connected with the bottom of reaction tower.
In some technical solutions：The output terminal of desalted water is connected by desalination water preheater with evaporation oxygen-eliminating device, described
Evaporation oxygen-eliminating device bottom an output terminal by low pressure feed water pump be connected successively with evaporator feedwater heater and evaporator,
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.
It is a kind of to be realized using above-mentioned device containing SO3The method of gas relieving haperacidity energy regenerating, this method are included with step：
(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 subsequent processing processing of reaction rear molding pneumatic transmission after tower bottom converges；
(2) 85+10% high-temperature sulfuric acids go out evaporator rear portion and enter mixer, with low pressure feed water reduce acid it is dense after again into
Enter the SO in reaction tower cyclic absorption process gas3, remaining high-temperature concentrated sulfuric acid sequentially enter evaporation oxygen-eliminating device generate low steam,
It enters back into the heating of evaporator feedwater heater and is sent into low pressure feed water, entering the extraneous desalination being sent into of desalination water preheater heating
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 the above method：The pressure of low-pressure steam that evaporation oxygen-eliminating device generates in step (1) is 0.15 ± 0.05MPa, ring
The temperature of pump discharge high-temperature sulfuric acid is 190 ± 30 DEG C, the pressure that evaporator generates low-pressure steam is 0.8 ± 0.4MPa.
Pressure described in technical solution of the present invention is gauge pressure.
Beneficial effects of the present invention：
Contain SO using of the present invention3Gas relieving haperacidity energy recycle device and method are straight using the outer heat for sulfuric acid
It practices midwifery raw low-pressure steam, is then sent into process gas pipeline before reaction tower, substitute section mixer and add water, reduce the work of mixer
Make load, reduce recycle acid flow, reduce the power consumption of circulating pump, it is often more important that in the situation in addition not consuming energy
Under, the heat of low steam (0.15 ± 0.05MPa) 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).Can real low-heat recovery system often produce 1 ton of sulfuric acid can be secondary
Produce 0.55 ± 0.1 ton of low-pressure steam.
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：
Such as Fig. 1, one kind contains SO3Gas relieving haperacidity energy recycle device, the device include reaction tower (1), evaporator (3), steam
Device feed-water heater (5) and evaporation oxygen-eliminating device (6) are sent out, the bottom of the reaction tower (1) passes through circulating pump (2) and evaporator
(3) be connected, an output terminal of evaporator (3) is connected by mixer (4) with the top of reaction tower (1), evaporator (3) it is another
One output terminal is connected successively with evaporation oxygen-eliminating device (6), evaporator feedwater heater (5) and desalination water preheater (7) is connected, and contains
SO3The output channel of process gas be connected with the bottom of reaction tower (1).The input terminal of desalted water passes through desalination water preheater
(7) be connected with evaporation oxygen-eliminating device (6), the output terminal of described evaporation oxygen-eliminating device (6) bottom by low pressure feed water pump (8) according to
Secondary to be connected with evaporator feedwater heater (5) with the input terminal of evaporator (3), another output terminal is pumped (8) by low pressure feed water
It is connected with mixer (4).Output terminal at the top of the evaporation oxygen-eliminating device (6) is with containing SO3Process gas output channel phase
Even.
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 in mass ratio 30:1 mixes, part SO in process gas3The gas temperature raising of generation sulfur process is reacted with low-pressure steam,
Process gas body temperature is 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, reaction life
Evaporator (3) is sent into after circulating pump (2) pressurization generate 0.6MPa's (g) into 200 DEG C of high-temperature sulfuric acids after tower bottom converges
Low-pressure steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
75% 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, remaining high-temperature sulfuric acid is picked out from evaporator outlet recycle acid pipeline, first
Into evaporation oxygen-eliminating device (6) thermal de-aeration and low-pressure steam 0.1MPa is generated, evaporator feedwater heater (5) heating is entered back into and send
Enter low pressure feed water, finally enter desalination water preheater, preheat room temperature desalted water, outer confession sulfuric acid temperature drops to 100 DEG C and send downstream
Process processing.
The room temperature desalted water that the external world is sent into first is heated to 98 DEG C in desalination water preheater (7), is re-fed into evaporation oxygen-eliminating device
(6), 120 DEG C are heated to, thermal de-aeration generates 0.1MP (g) 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, 10% low pressure feed water
Mixer (4) is sent to reduce cycle acid concentration, remainder dispensing evaporator feedwater heater (5) is heated to 150 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 0.615 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 according to mass ratio 50:1 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 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, instead
210 DEG C of high-temperature sulfuric acid should be generated and be sent into evaporator (3) generation 0.8MPa after circulating pump (2) pressurization after tower bottom converges
(g) low-pressure steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
85% high-temperature sulfuric acid goes out evaporator (3), and major part enters mixer (4) afterwards, after reducing acid concentration with low pressure feed water
Enter back into the SO in reaction tower (1) cyclic absorption process gas3, remaining high-temperature sulfuric acid is from evaporator outlet recycle acid pipeline
It picks out, be introduced into evaporation oxygen-eliminating device (6) thermal de-aeration and generate low-pressure steam 0.15MPa (g), enter back into evaporator feedwater heating
Low pressure feed water is sent into device (5) heating, finally enters desalination water preheater, preheats room temperature desalted water, outer to be dropped to for sulfuric acid temperature
108 DEG C are sent downstream process to handle.
The room temperature desalted water that the external world is sent into first is heated to 105 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 (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, and remainder dispensing evaporator feedwater heater (5) is heated to 160 DEG C, is being sent into
Evaporator generates the low-pressure steam of 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 0.603 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 is 90 according to mass ratio:1 mixes, part SO in process gas3Generation sulfur process gas temperature is reacted with low-pressure steam
Raising, 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,
The high-temperature sulfuric acid that reaction generates 220 DEG C is sent into evaporator (3) generation 1.2MPa after tower bottom converges after circulating pump (2) pressurization
Low-pressure steam, reaction rear molding pneumatic transmission subsequent processing processing.
95% 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, remaining high-temperature sulfuric acid is picked out from evaporator outlet recycle acid pipeline, first
Into evaporation oxygen-eliminating device (6) thermal de-aeration and low-pressure steam 0.2MPa is generated, evaporator feedwater heater (5) heating is entered back into and send
Enter low pressure feed water, finally enter desalination water preheater, preheat room temperature desalted water, outer confession sulfuric acid temperature drops to 121 DEG C and send downstream
Process processing.
The room temperature desalted water that the external world is sent into first is heated to 115 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 10% low pressure is given
Water send mixer (4) to reduce cycle acid concentration, and remainder dispensing evaporator feedwater heater (5) is heated to 171 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 0.596 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),
Evaporator feedwater heater (5) and evaporation oxygen-eliminating device (6), the bottom of the reaction tower (1) passes through circulating pump (2) and evaporator
(3) be connected, an output terminal of evaporator (3) is connected by mixer (4) with the top of reaction tower (1), evaporator (3) it is another
One output terminal is connected successively with evaporation oxygen-eliminating device (6) and evaporator feedwater heater (5) and desalination water preheater (7), containing SO3
The output channel of process gas be 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 pump (8) is connected successively with evaporator feedwater heater (5) and evaporator (3), another output terminal is given by low pressure
Water pump (8) is connected with mixer (4).
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 |
|---|---|---|---|
| CN201820467862.9U CN207581359U (en) | 2018-04-02 | 2018-04-02 | One kind contains SO3Gas relieving haperacidity energy recycle device |
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|---|---|---|---|
| CN201820467862.9U CN207581359U (en) | 2018-04-02 | 2018-04-02 | One kind contains SO3Gas relieving haperacidity energy recycle device |
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| Publication Number | Publication Date |
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| CN207581359U true CN207581359U (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 CN201820467862.9U patent/CN207581359U/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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