CN202046878U - Simple and energy-saving sulfur recovery process unit adopting one-step method - Google Patents
Simple and energy-saving sulfur recovery process unit adopting one-step method Download PDFInfo
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- CN202046878U CN202046878U CN2011201007194U CN201120100719U CN202046878U CN 202046878 U CN202046878 U CN 202046878U CN 2011201007194 U CN2011201007194 U CN 2011201007194U CN 201120100719 U CN201120100719 U CN 201120100719U CN 202046878 U CN202046878 U CN 202046878U
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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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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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 utility model relates to a simple and energy-saving sulfur recovery process unit adopting a one-step method, which comprises an acid gas separator, an acid gas preheater, a reactor, steam drum, a sulfur condenser, a sulfur gas separator and a washing tower that are connected in sequence, an air preheater is arranged in front of the reactor, reaction gas of the reactor is two paths of gas coming from the acid gas preheater and the air preheater; the gas from the acid gas preheater is Klaus gas washed by low-temperature methanol, liquid such as water, methanol and the like carried in the gas is separated by the acid gas separator, and then the gas is mixed with redundant nitrogen from air until H2S concentration in the acid gas is three percent, and the pressure is 0.05MPa; and the gas from the air preheater is redundant instrument air from an air buffer tank.
Description
Affiliated technical field:
The utility model relates to a kind of the present invention and designs a kind of recovery technology of sulfur device, particularly a kind of simple energy-economized single stage method sulfur recovery process unit.
Background technology:
The commercial run of handling sulfur-bearing from sour gas generally is exactly that sulfocompound is generated solid sulfur by reaction, makes discharging gas reach environmental requirement, and is also different for how many treatment processs of sour gas sulfur-bearing.
Recovery sulphur from hydrogen sulfide containing sour gas, having: improvement Claus technology in industrial application; Low temperature Claus technology (for example Clinsulf, Sulfreen, Clauspol, MCRC, CBA); Catalyzed oxidation technology (for example SuperClaus, Selectox, Cansolv, Crystasulf, A.D.A, PDS).
Clinsulf technology is developed by Linde company, adopts appropriate catalyst to quicken the sulphur conversion reaction.Be H
2The S direct oxidation is the gas phase catalysis process of sulphur simple substance.Contain H
2The S sour gas is heated directly to about 220 ℃, delivers to the Clinsulf reactor with the air mixed of preheating, at this H
2The S direct oxidation by the dew-point temperature of a built-in cooling system conditioned reaction device temperature out a little more than sulphur, is passed to oiler feed with reaction heat and is produced middle pressure steam, and sulphur is separated out in the condenser in downstream.
The core of this technology is the inner-cooled reactor of Linde company exploitation.This reactor is divided into two portions, and inlet part is provided with a non-cooling adiabatic reactor, allows temperature of reaction to rise rapidly to improve speed of response.There is a catalytic bed lower section, in establish a tube exchanger, this interchanger provides effective cooling so that the reactor outlet temperature is reduced to the dew-point temperature that approaches sulphur, so just can generation sulphur as much as possible.Top not precooling of reactor is to be convenient to cleaning when being subjected in the charging impurity effect when catalyzer and to change, and guarantees to reach COS and CS by reacting heat energy
2Deng 300～320 ℃ required temperature of organic sulfide hydrolysis.
The utility model content:
The purpose of this utility model be by to the investigation of state, inside and outside desulfurization technology, analyze, digest and assimilate, contain the characteristics that the low and most factory of sulphur concentration exists tail gas and gas more than needed at sour gas, a kind of simple energy-economized single stage method sulfur recovery process unit is provided.
The technical solution of the utility model is as follows: a kind of simple energy-economized single stage method sulfur recovery process unit, comprise the sour gas separator, sour gas preheater, reactor, drum, sulfur condenser, sulphur gas separating device and the washing tower that connect successively, be provided with an air preheater before reactor, the reactant gases of described reactor is two strands of gases from described sour gas preheater and described air preheater; Wherein, the gas of described sour gas preheater is after Crouse's gas of low-temperature rectisol separates liquid such as the water that carries in the gas and methyl alcohol through described sour gas separator, to be mixed to H in the sour gas with the nitrogen more than needed that divides from sky
2S concentration is 3%, and pressure is 0.05MPa; The gas of described air preheater is the instrument air more than needed from the air cushioning jar.
The catalyzer that described reactor adopts is the A988 catalyst for recovering sulfur.
Described reactor is taken away heat by described drum, and the bed temperature of described reactor is controlled at 280-320 ℃, air speed 1000h
-1, the reactor outlet gas temperature is 298 ℃.
The temperature out of described sulfur condenser is 120-125 ℃.
Compare with other allied equipment, the beneficial effects of the utility model are:
1, adopt emptying end gas or factory nitrogen more than needed to the H in the sour gas
2S content is adjusted control, the simple and non-power consumption of flow process.
2, adopt oxygen-containing gas that factory's factory air more than needed, instrument air or other do not have influence to catalyzer as unstripped gas, further simplified flow process and reduced power consumption simultaneously.
3, adopt the A988 catalyst for recovering sulfur, directly single stage method generates sulphur, and operational path is simple.
4, raw material is low temperature washing device for methanol and factory's by-product gas, and cost and power consumption are all lower.
Description of drawings:
Fig. 1 is the utility model structural representation.
Among the figure, 1, the sour gas separator; 2, sour gas preheater; 3, air preheater; 4, reactor; 5, drum; 6, sulfur condenser; 7, sulphur gas separating device; 8, washing tower.
Embodiment:
Further specify the utility model below in conjunction with drawings and Examples.A kind of simple energy-economized single stage method sulfur recovery process unit, comprise the sour gas separator (1), sour gas preheater (2), reactor (4), drum (5), sulfur condenser (6), sulphur gas separating device (7) and the washing tower (8) that connect successively, be provided with an air preheater (3) before reactor, the reactant gases of described reactor (4) is two strands of gases from described sour gas preheater (2) and described air preheater (3); Wherein, the gas of described sour gas preheater is after Crouse's gas of low-temperature rectisol separates liquid such as the water that carries in the gas and methyl alcohol through described sour gas separator, to be mixed to H in the sour gas with the nitrogen more than needed that divides from sky
2S concentration is 3%, and pressure is 0.05MPa; The gas of described air preheater adopts factory's factory air more than needed, instrument air or other catalyzer not to be had the oxygen-containing gas of influence.
As shown in Figure 1, workflow of the present utility model is: from Crouse's gas (H in the butt of low-temperature rectisol
2S concentration 6%, pressure 0.08MPa) after sour gas separator (1) separates liquid such as the water that carries in the gas and methyl alcohol, be mixed to the nitrogen more than needed that divides from sky that concentration is 3% in the sour gas, pressure 0.05MPa, enter sour gas preheater (2) and be heated to 220 ℃, instrument air more than needed from the air cushioning jar passes through air preheater preheating (3) to 220 ℃, after mixing, two strands of gases enter reactor (4), reactor is taken away heat by drum (5), bed temperature is controlled at 280-320 ℃, air speed 1000h
-1The reactor outlet gas temperature is 298 ℃, gas goes out to enter behind the reactor sulfur condenser (6) and reclaims heat and simultaneously gas sulphur is condensed into liquid sulfur, the sulfur condenser temperature out is controlled at 120-125 ℃, the sulfur condenser liquid mixture of working off one's feeling vent one's spleen enters sulphur gas separating device (7) liquid sulfur and gas is separated, gas comes out to enter washing tower (8) from top, emptying after the washing cooling.Molten sulfur flows out operations such as entering the subsequent granulation packing from sulphur gas separating device bottom.
Claims (6)
1. simple energy-economized single stage method sulfur recovery process unit, comprise the sour gas separator, sour gas preheater, reactor, drum, sulfur condenser, sulphur gas separating device and the washing tower that connect successively, it is characterized in that: be provided with an air preheater before reactor, the reactant gases of described reactor is two strands of gases from described sour gas preheater and described air preheater.
2. simple energy-economized single stage method sulfur recovery process unit according to claim 1 is characterized in that, the catalyzer that described reactor adopts is the A988 catalyst for recovering sulfur.
3. simple energy-economized single stage method sulfur recovery process unit according to claim 1 and 2 is characterized in that described reactor is taken away heat by described drum, and the bed temperature of described reactor is controlled at 280-320 ℃, air speed 1000h
-1, the reactor outlet gas temperature is 298 ℃.
4. simple energy-economized single stage method sulfur recovery process unit according to claim 1 and 2 is characterized in that the temperature out of described sulfur condenser is 120-125 ℃.
5. simple energy-economized single stage method sulfur recovery process unit according to claim 1 is characterized in that the gas of described air preheater is the instrument air more than needed from the air cushioning jar, or factory air.
6. simple energy-economized single stage method sulfur recovery process unit according to claim 1 is characterized in that described dilution gas is emptying end gas or rare gas element more than needed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201007194U CN202046878U (en) | 2011-04-08 | 2011-04-08 | Simple and energy-saving sulfur recovery process unit adopting one-step method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011201007194U CN202046878U (en) | 2011-04-08 | 2011-04-08 | Simple and energy-saving sulfur recovery process unit adopting one-step method |
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| CN202046878U true CN202046878U (en) | 2011-11-23 |
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| CN2011201007194U Expired - Fee Related CN202046878U (en) | 2011-04-08 | 2011-04-08 | Simple and energy-saving sulfur recovery process unit adopting one-step method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007746A (en) * | 2012-12-20 | 2013-04-03 | 济南承乾工程技术有限公司 | System for desorbing H2S in transform gas |
| CN104138713A (en) * | 2013-05-10 | 2014-11-12 | 杭州林达化工技术工程有限公司 | Method, device and reactor for recovery of sulfur from acidic gas |
-
2011
- 2011-04-08 CN CN2011201007194U patent/CN202046878U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007746A (en) * | 2012-12-20 | 2013-04-03 | 济南承乾工程技术有限公司 | System for desorbing H2S in transform gas |
| CN104138713A (en) * | 2013-05-10 | 2014-11-12 | 杭州林达化工技术工程有限公司 | Method, device and reactor for recovery of sulfur from acidic gas |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20111123 Termination date: 20130408 |