CA2461624C

CA2461624C - Process for producing nickel carbonyl, nickel powder and use thereof

Info

Publication number: CA2461624C
Application number: CA002461624A
Authority: CA
Inventors: Kamran M. Khozan; Dmitri S. Terekhov; Victor Emmanuel Nanthakumar; Sergiy Kovtun
Original assignee: Chemical Vapour Metal Refining Inc
Current assignee: CVMR Corp
Priority date: 2003-03-27
Filing date: 2004-03-22
Publication date: 2005-10-18
Anticipated expiration: 2024-03-22
Also published as: ZA200402339B; GB2425130B; AU2004201188B8; GB0406594D0; CA2461624A1; GB0606438D0; GB2399815A; AU2004201188B2; GB2425130A; GB2399815B; AU2004201188A1

Abstract

A process for producing Ni(CO)4 from carbon monoxide and a source of nickel selected from the group consisting of elemental nickel, a nickel compound or mixtures thereof, provided the nickel compound is not nickel chloride per se or in admixture with a nickel carbonate ore, in an amount greater than 50% W/W nickel chloride; which process comprises (a) treating the nickel source with hydrogen at a pressure of at least atmospheric pressure and an effective temperature, in the presence of chloride anion or an in situ generator thereof precursor, to produce a resultant nickel; (b) reacting the carbon monoxide with the resultant nickel to produce the Ni(CO)4; and collecting the Ni(CO)4. The process offers the production of Ni(CO)4 at atmospheric pressure and at a sufficiently high rate for direct use in subsequent deposition processes without the need for storage facilities.

Description

PROCESS FQR PRODUCING NICKEL CA~ONYL.
NICKEL POWDER AND USE TI~REOF
S FIELD OF THE INVENTION
This invention relates to processes for producing nickel carbonyl, more particularly to producing nickel powders of use in producing said nickel carbonyl by reaction with carbon monoxide, and to said nickel powders made by said process.
BACKGROUND TO THE INVENTION
Nickel carbonyl, Ni(CO)4 was first produced by the reaction of metallic nickel with carbon monoxide by Mond in the early part of the 19'" century. Today, one of the major industrial processes for making metallic nickel is,based on the production of Ni(CO)4 and subsequent thermal decomposition thereof to Ni and CO. One known commercial process operates at about 180°C and a CO pressure of about 70 atm. It is known that the CO pressure may be reduced when the reactant nickel is catalytically activated.
Activation of the metal has been observed in the presence of mercury (1, 2), sulfur in the form of H2S (3, 4), hydrogen (5, 6) or carbon (7). It has been suggested that the high initial rate of formation of Ni(CO)4 and the subsequent decline to a steady state value is the result of a rapid decrease in the number of activated reaction sites which are produced upon heat treatment of the sample (8, 9, 6). A study of surface changes during carbonyl synthesis suggests that the maximum rate is associated with fundamental changes in the defect structure. All of the above methods use catalytic activation of nickel in the presence of CO.
However, it can be readily appreciated that processes that at atmospheric pressure can produce nickel, particularly, activated nickel for subsequent reaction with CO at atmospheric pressure would provide signif cant capital and operating cost advantages.
Further, it can also be appreciated that processes that enable Ni(CO)4 to be manufactured at a su~cient rate as to obviate the need for storage in order to build up a sui~tcient supply for practical, eilxcient use in a subsequent nickel deposition process, would also offer significant capital and operating cost savings. To-date, in commercial operations rate limitations on the production of Ni(CO)4 require such storage facilities and operations.
S There is, thus, a desire for an improved method of Ni(CO)4 production which is operable at atmospheric pr~essm~e and which is of a sufficient rate as to negate the need for storage of the Ni(CO)4 prior to use in a subsequent decomposition and/or deposition process.
PUBLICATIQNS
1. Morton J.R., Preston K. F. J. Clam. Phys., 81, S6, (1984).

2. Morton J.R., Preston K. F. luorg. Chem., 24, 3317, (1985).

3. Mercer D. L.; Into Ltd. (Can. 1038169 (1975/78]).
1 S 4. Schafer H. ~ Anorg Allg. Chem. 493, 17 ( 1982).
5. Job R. J. Chem. Educ. 56, S56 (1979).
6. Mazurek H., Mehta R. S., Dresselhaus M. S., Dresselhaus G., Zeiger H. J.
Surf. Sci. 118, S30 (1982).
7. Korenev A. V., Shvartsman R. A., Mnukhin A. S., Tsvetn. Met. 1979 Nol l, pp. 37.
8. Mehta R. S., Dresselhaus M. S., Dresselhaus G., Zeiger H. J. Surf. Sci. 78, L681 ( 1978).
9. Greiner G., Manzel D. J. Caxal. 77 382 (1982).

It is an object of the present invention to provide a process for the commercial production of Ni(CO)4 from a source of nickel in an efficacious manner at atmospheric pressure, with resultant capital and operating cost savings.
It is a further object of the present invention to provide a process and apparatus for the commercial continuous production of Ni(CO)4 from a source of nickel at a sufficiently high rate as to negate the need for storage of the Ni(CO)4 prior to a subsequent decomposition step, with resultant capital and operating cost savings.

' Accordingly, in one aspect the invention provides a process for producing Ni(CO)4 fmm carbon monoxide and a source of nickel selected from the group consisting of elemental nickel, a nickel compound or mixtures thereof, provided said nickel compound is not nickel chloride her se or in admixture with a nickel carbonate ore in an amount greater than 50% w/w nickel chloride which process comprises (a) treating said nickel source with hydrogen at a pressure of at least atmospheric pressure and an effective temperature, in the presence of chloride anion or an ~ situ generator thereof precursor; to produce a resultant active nickel; and (b) reacting said carbon monoxide with said resultant active nickel to produce said Ni(CO)4.
By the term "resultant active nickel" as used in this specification and claims is meant resultant particulate nickel that reacts with CO at essentially atmospheric pressure and a temperature of from ambient (20°C) to 80°C to effect conversion to Ni(CO)4 at an acceptable conversion rate, By the term "acceptable conversion rate" is meant herein the rate of production of Ni(CO)4 in ~e order of at least 0.1 g/hr Ni(CO~ per g/Ni, which provides an efficacious rate for direct utilization, without the need for a build-up in storage, preferably for use in a commercial subsequent deposition process. A
more acceptable rate is 1 g/hr Ni(CO)4 per g/Ni and a still more advantageous rate is the maximum rate of 3.0 g/hr. Ni(CO)4 per g/Ni.
The effective temperature is a temperature which ,effects the production of resultant active nickel at an acceptable rate . of at least atmospheric pressure.
Preferably, the effective temperature is in the range 300° -650°C and more preferably, 350°- 550°C.
The Ni(CO)4 produced in step (b) may be collected, or, alternatively, when made at an acceptable conversion rate, as herein defined, preferably of at least 0.25 g/hr Ni(CO)4 per g Ni, preferably, at a rate of 3.0 g/hr Ni(CO)4 per g Ni directly passed to a deposition chamber for immediate decomposition to Ni and CO. This enables the CO to be immediately recycled in a close-loop manner as to provide a continuous CO closed-loop process.
Accordingly, in a further aspect, the invention provides an improved apparatus for the production of nickel powder, coatings, articles or compounds from the decomposition of Ni(CO)4, said apparatus comprising:-(a) a decomposition chamber having a Ni(CO)4 feed inlet, a spent CO outlet and adapted to receive a substrate;
(b) a Ni(CO~ production chamber having a CO feed inlet, a gaseous Ni(CO)4 product outlet and adapted to receive source nickel for reaction with CO, wherein the im~oved apparatus comprises (i) Ni(CO)4 direct feed means between said Ni(CO)4 feed inlet of said decomposition chamber for feeding Ni(CO)4 directly from said production chamber to said decomposition chamber at an acceptable feed rate:
(ii) CO recycle conduit means between said spent CO outlet and said CO
feed inlet; and (iii)wherein said source nickel comprises activated nickel produced as hereinabove defined.
Present prior art processes have very low conversion rates, typically of Iess than 0.03 g Ni(CO)4 /hr: per glNi, which requires that the Ni(CO)4 needs to be stored to a required volume prior to use in a subsequent decomposition or deposition step.
The nickel compounds of use in the practise of the invention as hereinabove defined may readily be selected, from, but not limited to, for example, the group consisting of a nickel salt, most particularly, nickel chloride, carbonate, hydroxide, oxide and metallic elemental nickel. The metallic elemental nickel is most preferably in particulate form, for example, as a very fine powder.
The preferred nickel salt is nickel chloride, preferably in the form of a hydrate, or a mixture thereof with nickel carbonate in the fonm of zaratite (2Ni(OH~-NiC03.4H20), preferably wherein the amount of nickel chloride is such as to produce 20 - 25% W!W of chloride based on nickel in the mixture.
The chloride anion may be selected from, by way of example, but not limited to, hydrogen chloride and a metallic chloride salt, such as, for example, an alkali, alkaline earth or transition metal simple or complex sait, e.g. FeCl3. The invention also includes processes that involve the use of precursors of chloride ion under the reaction conditions defined, such as, for example, suitable use of C12, oxides of chlorine gas and 'OCI3 salts that produce chloride anion in situ.
The chloride anion is, preferably, present at a ratio of at least 1:10 atomic W/W% Cf to Ni, more preferably 1:5 atomic W/W%.

4 A preferred process is wherein the chloride anion is present as gaseous hydrochloric acid in gaseous admixture with the hydrogen, and more preferably, wherein the nickel compound is first treated with hydrogen at the effective temperature for a first period of time and subsequently treated with the gaseous admixture for a second period of time, at the effective temperature.
The chloride anion in alternative embodiments may be gentratod in situ under the aforesaid process conditions, according to the invention as defined, in requisite effective amounts from chloride anion generating precursors, such as, for example, chlorate compounds and chlorine gns.
IO In a further aspect, the invention provides the resultant active nickel when made by a process as hereinabove defcned prior to its subsequent reaction with CO to form Ni(CO)4.
In a yet further aspect, the invention provides a process as hereinabove defined for producing resultant nickel from the decomposition of nickel carbonyl produced by I S a process as hereinabove defined.
We have found, further, that relatively small amounts of metal chlorides, e.g.
fendc chloride in the presence of non-chloride nickel compounds enable activated nickel to be formed according to the process of the invention as hereinabove defined.
The bus product stream comprises H2 and HCl and, optionally, H20, C02 20 and CO.
BRIEF DESCRIPTION OF THE DRAWINGS
In order that the invention may be better understood, preferred embodiments will now be described by way of example only with reference to the accompanying 25 drawing, wherein:-Fig. I is a graph showing overall conversion ('/o) against reaction time (hr.) for various processes according to the invention;
Fig. 2 is a diagrammatic flow diagram of a continuous self-contained process according to the invention; and 30 Fig. 3 is a diagrammatic sketch of a Ni(CO)4 production reaction chamber in direct communication with a Ni deposition chamber according to the invention.

5 DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
In order that the invention may be better understood, preferred embodiments will now be described by way of example only, wherein Examples 1 and 2 do not constitute part of the invention as claimed but are provided for comparison purposes only.
Exatgple 1 (Prior Art) NiC03 powder (200 g) was placed in an extraction reactor and treated with a stream of H2 gas at 300 rnL/rnin flow rate, at 500°C for 7 hours to effect substantially complete reduction. The nickel powder produced was cooled to 100°C and the atmosphere of H2 was subsequently replaced with carbon monoxide. The reactor was cooled further to 50°C and CO gas passed through at 300 mL/min flow rate. The resulting Ni(CO)4 was passed through a pair of carbonyl decomposers according to the prior art and nickel was recovered as nickel powder, (10 g; 10 % yield) after 12 hours.
Example 2 (Prior Art) Ni(OH}~ powder (100 g) was placed in the extraction reactor and treated with a stream of H2 gas at 300 mL/min flow, at 500°C for 7 hours to essentially complete reduction. The resulting nickel powder was cooled to 100°C in the atmosphere of H2 which was subsequently replaced with carbon monoxide. The reactor was cooled down further to 50°C and CO gas passed through at 300 mlr/min flow rate. The resulting Ni(CO)4 gas was passed through carbonyl decomposers and nickel powder (Gg, 9.5 yield) after 12 hours was recovered.
Examvle 3 300.1g of a nickel carbonate) nickel chloride mixture (10:1 w/w) was placed into an extraction n~ctor and treated with hydrogen (2L/min) at 450°C
for 6 hours.
Subsequently, the hydrogen was replaced with argon, the reactor cooled to 40°C and the argon replaced with carbon monoxide at a gas temperature of 80°C, and flow rate of 4 L/min. whereby nickel carbonyl was formed, collected and subsequently decomposed to Ni and CO to provide (1038; 70%) yield of nickel extraction yield in 6 hr.

6 302.3 g of the same mixture as in Example 3 was under similar conditions but wherein after 0.5 h, the hydrogen gas was doped with 1% of HCI for a further reaction period of 4 hours. The subsequent nickel extraction procedure was similar to Example 3 and gave 134g; 90% yield of nickel in 6 h.
Exain~le 5 300.1 g of nickel carbonate was treated under similar conditions as in Example 4 but wherein after 0.5 h a flow of 900cc/min of HCl gas was introduced into the hydrogen flow at 2 L/min for 4 h. The subsequent nickel extraction procedure was similar to Example 3 and gave a 96.48 % yield of nickel in 13 h.
The aforesaid examples 3-5 are better illustrated with reference to Fig. 1 wherein:-Line 1 represents the catbonylation of nickel produced by the reaction of a mixture of nickel cacbonate/nickel chloride 10:1. (6 h, 70.4% yield) according to Example 3.
Line 2 represents the same composition according to line 1 plus 1% pf HC1 in the gas stream (6 hours, 90.45% yield) according to Example 4; and Line 3 represents 100% nickel carbonate plus HCl (13 h, 96.48%) according to Example 5.
The aforesaid examples clearly illustrate the beneficial effect of having chloride anion present in admixture with a nickel compound in the hydrogen reactor in producing a particulate nickel more efficacious in reacting with CO to produce Ni(CO),,.

ExampleNi CompoundEquivalentDepositedTime Rate** Rate***

(g) Ni(g) Ni(g) (hr)*gNi/gNi/hrNi(CO)4 rox. / Ni/hr # 1 200 (NiC03)98 10 12 0.01 0.3 #2 100 (Ni(OH2))63 6 12 0.01 0.03 #3 300 NiC03 147 103 6 0.12 0.36 /

Ni C12 (10:1) #4 302 NiC03 148 134 6 0.15 0.45 /

Ni C12 (10:1) #5 300 g NiC03148 142 13 0.07 0.21

7 * carbonylation and subsequent decomposition time from treated (reduced) Ni.
** rate of deposition of Ni metal per se per hour per 1 gm equivalent Ni, calculated ~ from Ni compound starting material.
* * * Rate of production of Ni(CO)4 per hr. per g Ni.
Table 1 shows the beneficial enhancement in the rate of production of Ni from its various sources by the process according to the present invention, wherein the presence of chloride anion in Examples 3, 4 and 5 shows the very significant beneficial egect over the abs~ce of chloride anion in Examples l and 2.
This enhancement in production rate of Ni(CO)4 enables the direct use thereof in any subsequent desired decomposition step. .
Fig. 2 is a diagrammatic flow diagram of a continuous nickel deposition process self-contained with respect to CO, according to the invention. It shows generally as 10, a reaction chamber 12 linked to decomposition chamber 14 by Ni(CO)4 and CO conduits 16 and 18, respectively.
Chamber 12 contains, alternatively, nickel source 20 and resultant nickel 22;
and has hydrogen feed and outlet/recycle conduits 24 and 26, respectively; HCl feed and outlet/recycle conduits 28 and 30, respectively; and Ni(CO)4/CO exit conduit 16.
Decomposition chamber 14 contains a substrate 32 to be nickel coated from line 16.
In operation, nickel source 20 is treated with hydrogen, typically, at 400-500 °C for S-15 hours and 2 Umin at atmosphere pressure to produce a reduced nickel powder 21.
HCl gas at 1 Umin and 50 - 80° is then recycled through chamber I2, optionally, with hydrogen, to produce treated nickel powder 22. Chamber 12 is then subsequently purged with, for example, argon from conduit 23 and, thereafter, CO
from conduit 18 is fed into chamber 12, wherein Ni(CO~ is produced and passed through conduit 16 to decomposition chamber 14. Recycle conduit as shown in Fig. 2 are utilized as desired.
It can be seen that once the pmcess is operating at "steady state" for an alternative two-stage operative cycle, that the amount of CO used in the production of Ni(CO)4 can be met from ~e decomposition thereof in chamber 14. The process can thus be considered as being essentially self-contained with respect to CO.

8 Importantly, since the rate of praluction of Ni(CO)4 in chamber 12 is sufficiently high enough to warrant a direct feed to chamber 14 for decomposition of Ni onto substrate 32 in an efficacious manner, no intervening storage facility is required. This is of value in commercial operations.
Fig. 3 shows generally as 100 a double chamber apparatus for the continuous production and decomposition of Ni(CO)4.
Ni(CO)4 production chamber 120 contains activated nickel 140 prepared according to the invention, either in an initial starting amount as shown in this embodiment or under continuous feed means of an alternative embodiment (not shown). Chamber 120 has a CO feed inlet 160, whereby in operation CO gas reacts with nickel 140 to produce Ni(CO)4 at an acceptable production rate selected from 0.1 to 3.0 gNi(CO)4/g activated Ni/hr.
Decomposition chamber 180 contains a mandrel, mold or like substrate 200 having a substrate surface 220 upon which is deposited Ni as a coating 240 which constitutes a Ni shelf product in the embodiment shown by decomposition of gaseous Ni(CO)4 from chamber 120 fed through conduit 260. By-product CO exits chamber 180 through outlet 280 and is recycled through conduit 300 to feed inlet 160.
The above process constitutes a continuous, CO self contained system wherein the Ni(CO)4 is essentially produced in chamber 120 at a rate sufficient to provide for the practical deposition operation in chamber 180 as to negate the need for Ni(CO)4 storage with its attendant capital and operating costs.
Although this disclosure has described and illustrated certain preferred embodiments of the invention, it is to be understood that the invention is not restricted to those particular embodiments. Rather, the invention includes all embodiments which are functional or mechanical equivalents of the specific embodiments and features that have been described and illustrated.

9

Claims

1. A process for producing Ni(CO)4 from carbon monoxide and a source of nickel selected from the group consisting of elemental nickel, a nickel compound and mixtures thereof, provided said nickel compound is not nickel chloride per se or in admixture with a nickel carbonate ore in an amount greater than 50% w/w nickel chloride which process comprises (a) treating said nickel source with hydrogen at a pressure of at least atmospheric pressure and an effective temperature, in the presence of chloride anion or an in situ generator thereof precursor; to produce a resultant active nickel; and (b) reacting said carbon monoxide with said resultant active nickel to produce said Ni(CO)4.

2. A process as defined in claim 1 wherein said nickel compound is selected from the group consisting of a nickel salt, nickel hydroxide, nickel carbonate and nickel oxide.

3. A process as defined in claim 1 or claim 2 wherein said chloride anion is present from a compound selected from hydrogen chloride and a metallic chloride.

4. A process as defined in any one of claims 1 to 3 wherein said metallic chloride is selected from the group consisting of an alkali, alkaline earth and transition metal chloride.

5. A process as defined in any one of claims 1 to 4 wherein said chloride anion is present as gaseous hydrochloric acid in gaseous admixture with said hydrogen.

6. A process as defined in any one of claims 1 to 5 wherein said nickel compound is first treated with hydrogen at said effective temperature for a first period of time and subsequently treated with said gaseous admixture for a second period of time, at said effective temperature.

7. A process as defined in claim 5 or claim 6 wherein said nickel compound comprises nickel carbonate and said gaseous admixture comprises HCl and H2 in the molar ratio of about 1:2.

8. A process as defined in any one of claims 1 to 7 wherein said nickel compound is nickel carbonate.

9. A process as defined in any one of claims 1 to 8 wherein said effective temperature is selected from the range 300° - 650°C.

10. A process as defined in claim 9 wherein said effective temperature is selected from 350° - 550°C.

11. A process as defined in any one of claims 1 to 10 wherein said resultant active nickel is reacted with carbon monoxide at a temperature of about 50°C.

12. A process as defined in any one of claims 1 to 11 wherein said Ni(CO)4 is produced in step (b) at an acceptable conversion rate, and further comprising passing said Ni(CO)4 directly to a decomposition chamber and decomposing said Ni(CO)4 to deposit nickel and CO.

13. A process as defined in claim 12, wherein said decomposition effects deposition of Ni.

14.A process as defined in claim 12 or claim 13 wherein said acceptable conversion rate produce Ni(CO)4 at a rate of at least 0.1 g/hr Ni(CO)4 per g Ni.

15. A process as defined in claim 14 wherein said acceptable conversion rate is at least 0.25 g/hr Ni(CO)4 per g Ni,

16. A process as defined in claim 15 wherein said acceptable conversion rate produces Ni(CO)4 at a rate of 3.0 g/hr. Ni(CO)4 per g Ni.

17. A process as defined in any one of claims 1 to 16 wherein said precursor is selected from the group consisting of Cl2, oxides of chlorine and NaOCl.

18. A process for producing a resultant active nickel compound of subsequent use in the production of Ni(CO)4 by reaction with carbon monoxide, from a nickel source selected from the group consisting of elemental nickel, a nickel compound or mixtures thereof, which process comprises (a) treating said nickel source with hydrogen at a pressure of at least atmospheric pressure and an effective temperature, in the presence of chloride anion or an in situ generator thereof precursor as defined in any one of claims 1 to 17; and collecting said resultant active nickel.

19. An improved apparatus for the production of nickel powder, coatings, articles or compounds from the decomposition of Ni(CO)4, said apparatus comprising:-(a) a decomposition chamber having a Ni(CO)4 feed inlet, a spent CO outlet and adapted to receive a substrate;

(b) a Ni(CO)4 production chamber having a CO feed inlet, a gaseous Ni(CO)4 product outlet and adapted to receive source nickel for reaction with CO, wherein the improved apparatus comprises (i) Ni(CO)a direct feed means between said Ni(CO)4 feed inlet of said decomposition chamber for feeding Ni(CO)4 directly from said production chamber to said decomposition chamber at an acceptable feed rate:
(ii) CO recycle conduit means between said spent CO outlet and said CO
feed inlet; and (iii)wherein said source nickel comprises activated nickel produced according to any one of claims 1 to 18.
'0. Apparatus as defined in claim 19 wherein said direct feed means comprises means for feeding said Ni(CO)4 to said decomposition chamber at a rate of at least 0.1 g/hr. Ni(CO)4 per g said source nickel.