CN207524980U - A kind of relieving haperacidity energy recycle device of gas containing SO3 - Google Patents
A kind of relieving haperacidity energy recycle device of gas containing SO3 Download PDFInfo
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- CN207524980U CN207524980U CN201820469971.4U CN201820469971U CN207524980U CN 207524980 U CN207524980 U CN 207524980U CN 201820469971 U CN201820469971 U CN 201820469971U CN 207524980 U CN207524980 U CN 207524980U
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Abstract
The utility model discloses one kind to contain S03Gas 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 containing SO for above-mentioned insufficient one kind that provides3Gas 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 and evaporation oxygen-eliminating device, the bottom of the reaction tower are connected by circulating pump with evaporator, and an output terminal of evaporator leads to
It crosses mixer with the top of reaction tower to be connected, another output terminal of evaporator removes respectively with evaporator feedwater heater and evaporation
Oxygen device is connected, and the output terminal of the evaporator feedwater heater and evaporation oxygen-eliminating device is connected with desalination water preheater, containing SO3's
The output channel of process gas is 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 the evaporation oxygen-eliminating device bottom passes sequentially through low pressure feed water pump, 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, this method are included 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 goes out evaporator rear portion and enters mixer, with low pressure feed water reduce acid it is dense after
Enter back into the SO in reaction tower cyclic absorption process gas3, remaining high-temperature sulfuric acid is again split into two parts, 60 ± 40% into
Enter to evaporate oxygen-eliminating device thermal de-aeration and generate low-pressure steam, remainder enter evaporator feedwater heater heating be sent into low pressure to
Water, the sulfuric acid come out from evaporation oxygen-eliminating device and evaporator feedwater heater enters desalination water preheater, preheats 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 inlet ductwork and the SO in process gas3Reaction,
The deaerated water in oxygen-eliminating device is evaporated after low pressure feed water pump pressurization, and 25 ± 15% low pressure feed water send mixer reduction recycle acid dense
Degree, remainder dispensing evaporator feedwater heater, is re-fed into evaporator and generates low-pressure steam after heating.
In some specific technical solutions：The pressure of low-pressure steam that evaporation oxygen-eliminating device generates in step (1) is 0.15
± 0.05MPa, the temperature of circulating-pump outlet high-temperature sulfuric acid are 190 ± 30 DEG C, evaporator generate the pressure of low-pressure steam for 0.8 ±
0.4MPa。
The beneficial effects of the utility model：
Contain SO using described in the utility model3Gas relieving haperacidity energy recycle device, it is direct using the outer heat for sulfuric acid
Low-pressure steam is generated, is then sent into process gas pipeline before reaction tower, section mixer is substituted and adds water, reduce the work of mixer
Load reduces recycle acid flow, reduces 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 (g)) switchs to the heat for high temperature concentrated acid (190 ± 30 DEG C), and passes through evaporator
The middle low-pressure steam for generating more higher pressures (0.8 ± 0.4MPa (g)).Can real low-heat recovery system often produce 1 ton of sulfuric acid
It can be with 0.55 ± 0.1 ton of low-pressure steam of by-product.
Description of the drawings
Fig. 1 one kind contains SO3The 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 respectively with evaporator feedwater heater (5) with evaporation oxygen-eliminating device (6), the evaporator feedwater heater
(5) it is connected with the output terminal of evaporation oxygen-eliminating device (6) with desalination water preheater (7), containing SO3Process gas output channel with
The bottom of reaction tower (1) is connected.Extraneous desalination water end (W.E.) is connected by desalination water preheater (7) with evaporation oxygen-eliminating device (6), described
An output terminal for evaporating oxygen-eliminating device (6) bottom pumps (8) successively with evaporator feedwater heater (5) with evaporating by low pressure feed water
The input terminal of device (3) is connected, another output terminal pumps (8) by low pressure feed water and is connected with mixer (4).The evaporation deoxygenation
Output terminal at the top of device (6) is with containing SO3The output channel of process gas be connected.
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 is 30 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 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,
The high-temperature sulfuric acid that reaction generates 200 DEG C is sent into evaporator (3) generation 0.6MPa after tower bottom converges after circulating pump (2) pressurization
(g) 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, is entered back into after reducing acid concentration with low pressure feed water
SO in reaction tower (1) cyclic absorption process gas3, remaining high-temperature sulfuric acid picks out from evaporator outlet recycle acid pipeline,
Two parts are further divided into, 40%, which enters evaporator feedwater heater (5), heats feeding low pressure feed water, and 60% enters evaporation oxygen-eliminating device
(6) thermal de-aeration and low-pressure steam 0.1MPa is generated, high-temperature concentrated sulfuric acid goes out evaporator feedwater heater (5) and evaporation oxygen-eliminating device
(6) room temperature desalted water is preheated, outer confession sulfuric acid temperature drops to 100 DEG C and send at downstream process with entrance desalination water preheater afterwards
Reason.
The room temperature desalted water that the external world is sent into first is heated to 95 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 low-pressure steams simultaneously, and low-pressure steam send reaction tower (1) import and process gas
SO in body3Reaction, after low pressure feed water pumps (8) pressurization, 10% low pressure feed water send mixed the deaerated water in evaporation oxygen-eliminating device (6)
Clutch (4) reduces cycle acid concentration, and remainder dispensing evaporator feedwater heater (5) is heated to 158 DEG C, is being sent into evaporator
Generate the low-pressure steam of 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 0.632 per ton
Ton low-pressure steam.
Embodiment 1-2
Containing SO3Process gas before reaction tower (1) is entered, the 0.15MPa low pressure first generated with evaporation oxygen-eliminating device (6) is steamed
Vapour presses 50:1 mass ratio mixes, part SO in process gas3The gas temperature raising of generation sulfur process is reacted with low-pressure steam,
Process gas temperature is 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, reaction
The high-temperature sulfuric acid of 210 DEG C of generation is sent into evaporator (3) after circulating pump (2) pressurization after tower bottom converges and generates the low of 0.8MPa
Press steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
85% high-temperature sulfuric acid goes out evaporator (3) and enters mixer (4) afterwards, is entered back into after reducing acid concentration with low pressure feed water
SO in reaction tower (1) cyclic absorption process gas3, remaining high-temperature sulfuric acid picks out from evaporator outlet recycle acid pipeline,
Two parts are further divided into, 40%, which enters evaporator feedwater heater (5), heats feeding low pressure feed water, and 60% enters evaporation oxygen-eliminating device
(6) thermal de-aeration and low-pressure steam 0.15MPa is generated, high temperature concentrated acid goes out evaporator feedwater heater (5) and evaporation oxygen-eliminating device (6)
Room temperature desalted water is preheated with entrance desalination water preheater afterwards, outer confession sulfuric acid temperature drops to 111 DEG C and downstream process is sent to handle.
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), 127 DEG C are heated to, thermal de-aeration generates 0.15MP low-pressure steams simultaneously, and low-pressure steam send reaction tower (1) import and technique
SO in gas3Reaction evaporates the deaerated water in oxygen-eliminating device (6) after low pressure feed water pumps (8) pressurization, and 20% low pressure feed water is sent
Mixer (4) reduces cycle acid concentration, and remainder dispensing evaporator feedwater heater (5) is heated to 163 DEG C, is re-fed into evaporation
Device 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 0.625 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
(g) low-pressure steam, the subsequent processing processing of reaction rear molding pneumatic transmission.
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 picks out from evaporator outlet recycle acid pipeline, then
It is divided into two parts, 40%, which enters evaporator feedwater heater (5), heats feeding low pressure feed water, and 60% enters evaporation oxygen-eliminating device
(6) thermal de-aeration and low-pressure steam 0.15MPa is generated, high-temperature concentrated sulfuric acid goes out evaporator feedwater heater (5) and evaporation oxygen-eliminating device
(6) room temperature desalted water is preheated, outer confession sulfuric acid temperature drops to 124 DEG C and send at downstream process with entrance desalination water preheater afterwards
Reason.
The room temperature desalted water that the external world is sent into first is heated to 107 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 176 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 0.608 per ton
Ton low-pressure steam.
Claims (3)
1. one kind contains S03Gas 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 respectively with evaporator feedwater heater (5) with evaporation oxygen-eliminating device (6), the evaporator feedwater heater
(5) it is connected with the output terminal of evaporation oxygen-eliminating device (6) with desalination water preheater (7), containing SO3Process gas output channel with
The bottom of reaction tower (1) is connected.
2. according to claim 1 contain S03Gas 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 is successively
(8) are pumped by low pressure feed water, evaporator feedwater heater (5) is connected with the input terminal of evaporator (3), another output terminal passes through
Low pressure feed water pump (8) is connected with mixer (4).
3. according to claim 1 contain S03Gas 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.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820469971.4U CN207524980U (en) | 2018-04-02 | 2018-04-02 | A kind of relieving haperacidity energy recycle device of gas containing SO3 |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201820469971.4U CN207524980U (en) | 2018-04-02 | 2018-04-02 | A kind of relieving haperacidity energy recycle device of gas containing SO3 |
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| CN207524980U true CN207524980U (en) | 2018-06-22 |
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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 CN201820469971.4U patent/CN207524980U/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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