[go: up one dir, main page]

WO1996003198A1 - Desulfuration de gaz non condensable provenant de la distillation sous vide de petrole brut - Google Patents

Desulfuration de gaz non condensable provenant de la distillation sous vide de petrole brut Download PDF

Info

Publication number
WO1996003198A1
WO1996003198A1 PCT/US1995/009290 US9509290W WO9603198A1 WO 1996003198 A1 WO1996003198 A1 WO 1996003198A1 US 9509290 W US9509290 W US 9509290W WO 9603198 A1 WO9603198 A1 WO 9603198A1
Authority
WO
WIPO (PCT)
Prior art keywords
column
section
fact
desulfurization
gas
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US1995/009290
Other languages
English (en)
Inventor
Jiri Zachoval
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Glitsch Inc
Original Assignee
Glitsch Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Glitsch Inc filed Critical Glitsch Inc
Priority to CZ97194A priority Critical patent/CZ19497A3/cs
Priority to JP8505898A priority patent/JPH10506364A/ja
Priority to KR1019970700411A priority patent/KR970704499A/ko
Priority to EP95928114A priority patent/EP0772485A4/fr
Priority to SK83-97A priority patent/SK8397A3/sk
Priority to AU31988/95A priority patent/AU3198895A/en
Publication of WO1996003198A1 publication Critical patent/WO1996003198A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • B01D53/14—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 by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/16—Fractionating columns in which vapour bubbles through liquid
    • B01D3/22—Fractionating columns in which vapour bubbles through liquid with horizontal sieve plates or grids; Construction of sieve plates or grids
    • 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
    • B01D53/14—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 by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1468—Removing hydrogen sulfide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00—Sulfur; Compounds thereof
    • C01B17/02—Preparation of sulfur; Purification
    • C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
    • C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
    • C01B17/0408—Pretreatment of the hydrogen sulfide containing gases

Definitions

  • This invention concerns apparatus and a process for the elimination of hydrogen sulfide from incondensible gases derived from the distillation under vacuum of heavy- fractions of crude oil.
  • Another difficulty is caused by the fact that the gases coming from the vacuum system are available at pressures only slightly above atmospheric, such that a desulfurization system must have extremely low pressure drop in order to allow the gas to be sent for combustion, without the need to resort to the use of compression systems.
  • the invention now proposed overcomes the previously- cited limitations and problems of the earlier technology, making available desulfurization apparatus and procedure for gas which contains H 2 S by the use of ammonia solutions.
  • the current invention is able to furnish recovery yields which are considerably higher with respect to those achievable by traditional methods.
  • An additional object of the invention is that of realizing desulfurization apparatus and process which enable the efficient removal of H 2 S, even without the use of quantities of ammonia in excess of the stoichiometric amount .
  • the invention also achieves the goal of realizing desulfurization apparatus and process with the use of ammonia solutions in which the desulfurized gases are completely free of NH 3 .
  • Another goal of the invention is that of realizing apparatus and process particularly adapted to obtain efficient desulfurization of gases with an ammonia solution at a pressure that is substantially atmospheric.
  • the invention has additionally the goal of providing for the efficient desulfurization of gases using a solution of ammonia, making available a process and apparatus which does not cause significant pressure drop in the gas stream that is being subjected to the desulfurization treatment.
  • an additional goal of the invention is that of realizing an apparatus provided with packing beds which are able to offer high mass transfer and also provided with a distribution device having an improved ability, with respect to traditional devices, to irrigate the packing beds in the column sections, while at the same time having simpler and more economical structure than the already known analogous devices.
  • the apparatus of the invention is further characterized by the fact that the said distribution device may include a ring that is positioned above the said cylindrical body and that is suitable to collect and distribute the liquid stream fed to the said first section of the column.
  • Both of the two sections of the desulfurizing column preferably are filled by random or stacked packing material such as sold under the trademark CASCADE MINI- RINGS ® or by structured packing such as the type sold under the trademark GEMPAK ® .
  • the current process provides:
  • the said second stage in which a gaseous stream liberated from the first stage is brought into contact with water, the aqueous solution resulting from the gas liquid contact in the said second stage being sent to the said first stage.
  • the said aqueous solution resulting from the said second stage is an ammonia solution obtained by contact between the water fed to the second stage and the ammonia entrained by the gas rising from the first stage.
  • the ammonia solution employed in the first stage contains the stoichiometric quantity of ammonia available for the reaction with the H 2 S contained in the said initial gas mixture.
  • the process of the invention is characterized further by the fact that the said initial gaseous mixture contains up to 500,000 ppm by weight of H 2 S, and the desulfurized gas contains from less than 1 to 10 ppm by weight of residual H 2 S.
  • the said process additionally is carried out at a pressure below 1500 mbar abs, and the pressure drop of the gaseous stream between the inlet and the outlet of the column is not above 15 mbar.
  • That of the invention offers the advantage of allowing the almost complete absorption of the said sulfur compound by the use of a stoichiometric quantity of ammonia.
  • the process of the invention furnishes desulfurized gases which are completely free of ammonia.
  • the absence of excess quantities of liquid introduced into the column allows for a liquid stream leaving the desulfurization unit to have a total volume which can be treated by the downstream units of the apparatus, without the need to install new equipment of larger capacity than those originally installed.
  • the current invention provides the surprising and unexpected result of allowing the effective application of packed columns (of the type more fully described in the following) as desulfurization columns operating at a pressure slightly above atmospheric.
  • packed columns of the type more fully described in the following
  • the current invention is particularly adapted to perform the desulfurization of incondensible gases coming from vacuum crude distillation units. These gases, after desulfurization, are reused in the furnaces of the same column.
  • the current invention thanks to the presence of the previously-mentioned distribution device, offers the advantage of providing notable irrigation of the packing bed, with 300-400 irrigation points per square meter, while leaving an open area for the passage of the gases equal to twenty to twenty-five percent of the total cross-sectional area of the column.
  • traditional towers with riser-style distributors in order to maintain the same area available for the passage of the gases, it has not been possible to obtain more than 60-65 irrigation points per square meter.
  • the distributor described herein offers in addition the advantage of having a very simple structure, which allows it to be inserted as a single cartridge into the column without requiring the internal supports or intermediate flanges normally necessary in traditional equipment .
  • Figure 1 illustrates a flow scheme of the invented apparatus.
  • FIG 2 illustrates in longitudinal cross-section the details of the desulfurization column of the apparatus in Figure 1.
  • Figure 3 illustrates the detail of the distribution device used in the column in Figure 2.
  • Figure 1 shows a knock out drum 1 for the separation of the liquid phase which generally is entrained in the gas stream 8 coming from a vacuum crude distillation column and from which it is desired to eliminate the H 2 S.
  • a desulfurization column 2 Above the knock out drum 1, mounted directly on top, is a desulfurization column 2. For the treatment of a refinery gas coming from apparatus processing 3,000,000 tons/year of crude oil, this column would typically have a diameter varying between 200 and 300 mm.
  • This column 2 Inside column 2 are two distinct sections, each having a single packed bed. A lower or first section 3 and an upper or second section 4 are positioned in cascade one above the other. Each of the sections is characterized by a portion containing a packing material.
  • the preferred packing material is the metal version of a type shown in patents GB 1 385 672 and GB 1 385 673. It is sold under the trademark CASCADE MINI-RINGS ® .
  • An alternative but also suitable type of packing material would be structured packing of the type sold under the trademark GEMPAK ® .
  • the first or lower section 3 of the column 2 effects the first stage of desulfurization, in which gas stream 14 from the knock out drum 1 is brought into countercurrent contract with a fresh ammonia solution 9.
  • Solution 9 contains a stoichiometric quantity of NH 3 that reacts with the H 2 S contained in the initial gas mixture. In this first stage an initial desulfurization of the gas to be treated is effected.
  • the gas stream 15 liberated by section 3 still contains a certain quantity of H 2 S.
  • Stream 15 also entrains part of the ammonia with which it entered into contact in the packing material of the first section 3.
  • the gas stream so composed enters the upper section 4 of the column 2, where it enters into countercurrent contact with a stream of water 10, again in a bed of packing material like that in section 3.
  • the H 2 S not removed in the first stage is absorbed, with the use of a quantity of ammonia which corresponds stoichiometrically to the composition of H 2 S in the gas stream 15 liberated from section 3 of the desulfurization column.
  • the sulfur-ammonia solution generated by section 4 of the column by contact between the water 10 and the gas stream 15 previously described, makes liquid stream 17 which in turn falls back into section 3 below, combining with that produced by the stream of ammonia solution 9.
  • the total sulfur ammonia liquid stream 16 exiting from the bottom of the column 2 falls into the knock out drum 1.
  • the upper section 4 of the column realizes the final desulfurization of the initial gas mixture, eliminating the traces of H 2 S not absorbed by the first stage 3.
  • This absorption is additionally achieved by using a quantity of ammonia (present in gas stream 15) which comes directly from the first stage and which for this reason is that which corresponds exactly, from the stoichiometric point of view, to the concentration of H 2 S in the gas exiting from the lower section 3 of the desulfurization column.
  • the desulfurized gas 11 which exits finally from the top of the column 2 has a content of H 2 S ranging from less than 1 ppm up to a maximum of 10 ppm by weight.
  • the desulfurized gas exiting from the column 2 does not contain any trace of NH 3 because it has reacted completely with the H 2 S in the initial gas mixture.
  • the final gas always contains a certain quantity of NH 3 , the elimination of which, as well as being necessary, is made particularly difficult due to the simultaneous presence of significant quantities of residual H 2 S in the treated gas mixture.
  • the desulfurized gases 11 still have sufficient pressure to be sent to the vacuum crude tower furnaces.
  • the method of construction indicated above has the advantage of reducing to the minimum the pressure drop (the reduction in pressure is in general less than 15 mbar) so as to make unnecessary the use of auxiliary compressors for the feeding of the desulfurized gas to the burners.
  • a liquid phase 12 which contains the condensate separated from the gas stream 8 coming from the vacuum column, plus the sulfur-ammonia solution 16 composed of monosulfide and bisulfide of ammonia, exiting from the bottom of the desulfurization column 2.
  • the quantity of the liquid phase 16 which comes from the desulfurization column 2 does not exceed usually ten percent of the total rate of the liquid 12 exiting the knock out drum.
  • the liquid stream 12 exiting the knock out drum 1 and being sent to the stripper 5 has a volume which does not exceed the design capacity of the latter, even in apparatus that existed prior to the installation of the column 2.
  • the gas fraction 13 separated by the stripper 5 is finally sent to the Claus unit for the recovery of the sulfur.
  • the desulfurization column 2 has inlets 6 and 7 for the input of ammonia solution 9 to section 3 and the water stream 10 to section 4 respectively. These liquid streams 9 and 10 are in turn received within the respective sections 3 and 4 by a distribution device 18 which is illustrated in Figure 3. It has been emphasized that the distributor illustrated in Figure 3 is designed to be mounted above section 3 of the column. The corresponding distributor 18 positioned above the section 4 of packing material differs from that of section 3 by the absence of a collector ring 19, which will be better described as follows.
  • the distribution device 18 includes a support 20, which may conveniently be formed of upper and lower cross bars 20a connected by four support rods 20b.
  • a cylindrical body 21, and above it a ring 19, are fixed on the four support rods.
  • the cylindrical body 21 has in particular a base 22 equipped with holes 23. It receives the liquid phases coming from above (water in the case of section 4 and ammonia solution 9 plus liquid stream 17 in section 3 ) and it distributes the liquid phases uniformly onto the packed beds present in the sections 3 and 4. With the distributor device 18 installed above section 4 of column 2, the water stream 10 fed to section 4 is received directly by the cylindrical body 21 described above.
  • a portion of the liquid stream fed to section 3 of the column is received above the cylindrical body 21 by the previously-mentioned collector ring 19, which has the function of collecting that portion of the stream of liquid 17 coming from section 4 that is near the wall of the column and distributing it into the body 21 below.
  • the ring 19 has a surface which is preferentially inclined toward the center of the column so as to favor the collection of the liquid 17 which adheres to the walls of the column and send it into the perforated cylindrical body 21 of the distributor 18.
  • the ring 19 advantageously has a larger diameter (for example 260 mm) than that of the body 21 below (for example 230 mm) , the difference representing the surface left open for the passage of gas, which is equivalent to twenty to twenty-five percent of the total available area.
  • the distributor 18 is mounted on a containment grid 24.
  • the distribution device 18 illustrated in Figure 3 is particularly well adapted to flanged columns of less than 900 mm diameter.
  • a column of diameter 300 mm had a first section 5 m high and a second section 3.3 m high. Both sections were equipped with 25 mm CASCADE MINI-RINGS ® packing material and were separated by a distributor of the type previously described. This distributor presented a collector ring having an external diameter of 300 mm. The cylindrical body had an external diameter of 265 mm. A second distributor at the top of the column was identical to the former one, but without the collector ring. Into this column was fed 300 kg/h of gases having the following percentage composition by weight.
  • a column of diameter 450 mm had an upper section 4 m high and a lower section 5.50 m high. Both these sections were equipped with GEMPAK ® structured packing. Between them a distributor was placed that was the same as the one described in Example 1, except that it had a cylindrical body having an external diameter of 390 mm and a collector ring having an external diameter of 450 mm.
  • the gas obtained at the top of the desulfurization column had a H 2 S content less than 10 ppm.
  • the gas pressure at the entrance of the column was measured at 1350 mbar, and the pressure at the top was 1335 mbar, yielding a pressure drop of 15 mbar.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Procédé et appareil de désulfuration du produit gazeux provenant de la distillation sous vide de la fraction lourde de pétrole brut. Le mélange gazeux de départ (8) à désulfurer est un gaz non condensable contenant de l'acide sulfhydrique. Une colonne de contact gaz/liquide (2) présente une première et une seconde parties (3, 4) contenant des lits de matière de garniture structurée ou aléatoire et disposés sous des dispositifs d'irrigation (18) qui en assurent l'humidification tout en n'occasionnant que des pertes minimes de pression dans le gaz traversant la colonne. Le mélange gazeux de départ (8) est séché puis introduit (14) dans la première partie (3) de la colonne avec une solution neuve de gaz ammoniac (9) en quantité stoechiométrique pour assurer la réaction avec la quantité d'acide sulfhydrique présente dans le mélange gazeux de départ. La première partie de la colonne reçoit enfin une deuxième solution de gaz ammoniac qu'on fait passer de la deuxième partie de la colonne dans la première partie.
PCT/US1995/009290 1994-07-22 1995-07-20 Desulfuration de gaz non condensable provenant de la distillation sous vide de petrole brut Ceased WO1996003198A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
CZ97194A CZ19497A3 (en) 1994-07-22 1995-07-20 Process and apparatus for desulfurizing non-condensable gases from crude oil distillation process
JP8505898A JPH10506364A (ja) 1994-07-22 1995-07-20 原油の減圧蒸留からの非凝縮性ガスの脱硫
KR1019970700411A KR970704499A (ko) 1994-07-22 1995-07-20 원유의 진공 증류시 발생하는 비응축성 가스의 탈유황 처리(desulfurization of incondensible gases from the vacuum distillation of crude oil)
EP95928114A EP0772485A4 (fr) 1994-07-22 1995-07-20 Desulfuration de gaz non condensable provenant de la distillation sous vide de petrole brut
SK83-97A SK8397A3 (en) 1994-07-22 1995-07-20 Device and method for desulfurization of incondensible gases from the vacuum distillation of crude oil
AU31988/95A AU3198895A (en) 1994-07-22 1995-07-20 Desulfurization of incondensible gases from the vacuum distillation of crude oil

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ITMI94A001549 1994-07-22
IT94MI001549A IT1276323B1 (it) 1994-07-22 1994-07-22 Procedimento ed impianto di desolforazione di gas contenenti h2s

Publications (1)

Publication Number Publication Date
WO1996003198A1 true WO1996003198A1 (fr) 1996-02-08

Family

ID=11369335

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1995/009290 Ceased WO1996003198A1 (fr) 1994-07-22 1995-07-20 Desulfuration de gaz non condensable provenant de la distillation sous vide de petrole brut

Country Status (12)

Country Link
EP (1) EP0772485A4 (fr)
JP (1) JPH10506364A (fr)
KR (1) KR970704499A (fr)
CN (1) CN1159767A (fr)
AU (1) AU3198895A (fr)
CA (1) CA2195631A1 (fr)
CZ (1) CZ19497A3 (fr)
HU (1) HUT76148A (fr)
IT (1) IT1276323B1 (fr)
PL (1) PL318272A1 (fr)
SK (1) SK8397A3 (fr)
WO (1) WO1996003198A1 (fr)

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2878099A (en) * 1955-07-22 1959-03-17 Ruhrstahl Ag Fa Method of deacidifying gases
US4263021A (en) * 1972-12-05 1981-04-21 The Babcock & Wilcox Company Gas-liquid contact system
US4297329A (en) * 1977-12-22 1981-10-27 Union Carbide Corporation Vapor-liquid contacting system
US4342731A (en) * 1980-06-13 1982-08-03 Dr. C. Otto & Comp. G.M.B.H. Method for removing hydrogen sulfide from coke oven gas
US4569832A (en) * 1982-03-12 1986-02-11 Firma Carl Still Gmbh & Co. Kg Method and apparatus for desulfurizing coke oven gases
US5389351A (en) * 1992-11-04 1995-02-14 Hasebe; Nobuyasu Method for desulfurizing a gas

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2901935C2 (de) * 1979-01-19 1986-01-09 Linde Ag, 6200 Wiesbaden Wärme- und Stoffaustauschkolonne
CH642566A5 (de) * 1979-10-25 1984-04-30 Sulzer Ag Trogartige vorrichtung zum sammeln und verteilen der fluessigkeit in einer gegenstromkolonne.

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2878099A (en) * 1955-07-22 1959-03-17 Ruhrstahl Ag Fa Method of deacidifying gases
US4263021A (en) * 1972-12-05 1981-04-21 The Babcock & Wilcox Company Gas-liquid contact system
US4297329A (en) * 1977-12-22 1981-10-27 Union Carbide Corporation Vapor-liquid contacting system
US4342731A (en) * 1980-06-13 1982-08-03 Dr. C. Otto & Comp. G.M.B.H. Method for removing hydrogen sulfide from coke oven gas
US4569832A (en) * 1982-03-12 1986-02-11 Firma Carl Still Gmbh & Co. Kg Method and apparatus for desulfurizing coke oven gases
US5389351A (en) * 1992-11-04 1995-02-14 Hasebe; Nobuyasu Method for desulfurizing a gas

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP0772485A4 *

Also Published As

Publication number Publication date
EP0772485A1 (fr) 1997-05-14
HUT76148A (en) 1997-07-28
AU3198895A (en) 1996-02-22
CA2195631A1 (fr) 1996-02-08
IT1276323B1 (it) 1997-10-28
SK8397A3 (en) 1997-07-09
JPH10506364A (ja) 1998-06-23
ITMI941549A0 (it) 1994-07-22
CN1159767A (zh) 1997-09-17
KR970704499A (ko) 1997-09-06
EP0772485A4 (fr) 1997-08-06
ITMI941549A1 (it) 1996-01-22
CZ19497A3 (en) 1997-07-16
PL318272A1 (en) 1997-05-26

Similar Documents

Publication Publication Date Title
US4678648A (en) Method and apparatus for selective absorption of hydrogen sulphide from gas streams containing hydrogen sulphide and carbon dioxide
US3966875A (en) Process for the desulfurization of gases
CA2971657C (fr) Appareillage et procede de desulfuration a l'ammoniac par ajout d'ammoniac dans des chambres differentes
US4280990A (en) High pressure process for recovery of sulphur from gases
KR880012483A (ko) 디클로로실란의 제조공정 및 장치
US4400363A (en) Method for the removal of sulfur oxides and nitrogen oxides from exhaust gases
US4487748A (en) Process for treating exhaust gases
US4412977A (en) Selective acid gas removal
JP2004535297A (ja) ガス流から酸性ガスを除去する方法
US20180296970A1 (en) Wet desulfurization process using a suspension bed
US4057403A (en) Gas treating process
JPH0345118B2 (fr)
US3862295A (en) Method for sorptive removal of sulfur gases
US3172725A (en) Production of sulfuric acid
US5147620A (en) Process for the purification of gaseous streams
CN101239272B (zh) 污水储罐排放气的处理方法
CA1092159A (fr) No translation available
JPH01304026A (ja) 高純度トリエタノールアミンを用いて流体混合物から硫化水素を選択的に除去する方法
US4894179A (en) Absorbent composition containing a tertiary amino azabicyclic alcohol and an amine salt
CN101239271A (zh) 酸性污水储罐排放气的净化处理方法
CN101837226A (zh) 吸收塔
JP3486696B2 (ja) 亜硫酸ガスを含むガスを被処理ガスとする脱硫方法
EP0772485A1 (fr) Desulfuration de gaz non condensable provenant de la distillation sous vide de petrole brut
CA2006093C (fr) Elimination de l'hydrogene sulfure dans un melange gazeux
US4407784A (en) Process for the selective extraction treatment of gaseous hydrocarbon mixture containing carbon dioxide

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 95194824.5

Country of ref document: CN

AK Designated states

Kind code of ref document: A1

Designated state(s): AU BR CA CN CZ HU JP KR MX PL RU SK TT US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LU MC NL PT SE

121 Ep: the epo has been informed by wipo that ep was designated in this application
DFPE Request for preliminary examination filed prior to expiration of 19th month from priority date (pct application filed before 20040101)
WWE Wipo information: entry into national phase

Ref document number: 8397

Country of ref document: SK

WWE Wipo information: entry into national phase

Ref document number: 2195631

Country of ref document: CA

Ref document number: PV1997-194

Country of ref document: CZ

WWE Wipo information: entry into national phase

Ref document number: 1019970700411

Country of ref document: KR

WWE Wipo information: entry into national phase

Ref document number: 1995928114

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 1997 776218

Country of ref document: US

Date of ref document: 19970424

Kind code of ref document: A

WWP Wipo information: published in national office

Ref document number: 1995928114

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: PV1997-194

Country of ref document: CZ

WWP Wipo information: published in national office

Ref document number: 1019970700411

Country of ref document: KR

WWR Wipo information: refused in national office

Ref document number: PV1997-194

Country of ref document: CZ

WWW Wipo information: withdrawn in national office

Ref document number: 1019970700411

Country of ref document: KR

WWW Wipo information: withdrawn in national office

Ref document number: 1995928114

Country of ref document: EP